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WO1986000920A1 - Procede pour eliminer les substances volatiles contenues dans l'eau produite par des procedes de valorisation du charbon - Google Patents

Procede pour eliminer les substances volatiles contenues dans l'eau produite par des procedes de valorisation du charbon Download PDF

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Publication number
WO1986000920A1
WO1986000920A1 PCT/EP1985/000297 EP8500297W WO8600920A1 WO 1986000920 A1 WO1986000920 A1 WO 1986000920A1 EP 8500297 W EP8500297 W EP 8500297W WO 8600920 A1 WO8600920 A1 WO 8600920A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
stripper
water
heat exchanger
direct heat
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/EP1985/000297
Other languages
German (de)
English (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 WO1986000920A1 publication Critical patent/WO1986000920A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0005—Degasification of liquids with one or more auxiliary substances
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
    • C02F1/586—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing ammoniacal nitrogen
    • 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
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention relates to a method for removing volatile ingredients such.
  • wash water and steam condensates enriched with volatile substances must be treated.
  • the removal of the volatile inorganic constituents from such waters is carried out on coal upgrading plants practically exclusively in abrasives which are operated with steam as the heating and carrier medium. As a result, water enters the process as steam condensate.
  • a temperature of at least 65 ° C is necessary in order to remove the compounds present in the ammonia water, for example Ammonium carbo- completely dissociate nate or ammonium sulfide. If you now operate such a stripper with a preheated gas and an ammonia water of the same temperature, the water will evaporate until the gas is saturated with water vapor. However, due to the high heat of vaporization of water, this leads to a strong cooling in the system. If you want to perform such a stripping process at 70 ° C and calculate with a gas-condensate ratio of 500 m 3 i. N. to 1 3 , then a heat of vaporization of approx.
  • He N. and K are preheated to approx. 600 ° C. This makes the use of high quality energy necessary.
  • the stripping gas is preheated by indirect heat exchange.
  • water vapor must be added to the stripping gas in order to avoid excessive cooling of the gas and thus a deterioration in the stripping effect. Also here, as with the other processes, it is necessary to add high-quality energy.
  • the object of the invention is to provide the gas used for stripping as inexpensively as possible.
  • the steam necessary for the processing of the process water can be partially or completely saved by treating the water loaded with the volatile compounds in a gas stripper instead of in an abortive device, the stripping gas being previously in a di right heat exchanger is heated and saturated with water vapor.
  • the operating temperature of the stripper is between 65 and
  • the water from the supply circuit of a coke oven battery, which is to be worked up in the stripper, contains 3.7 g NH./1, 0.73 g H ⁇ S / 1 and 35 mg HCN / 1 of volatile substances to be removed. There will be 25 m 3 / h of this template water 75 ° C through the lines 1, 2 and 3 to the head of the stripper 4. At the foot of the stripper 4, the purified water runs through lines 5 and 6. It still has a concentration of volatile ammonia of 72 mg / 1, of hydrogen sulfide of less than 1 mg / 1 and of hydrocyanic acid of 11 mg / 1.
  • This hot, water vapor-saturated air enters through lines 10 and 11 in the foot of the stripper 4, where it strips the template solution entering through line 3 in countercurrent, and leaves the stripper, enriched with the volatile substances, via lines 12 , 13 and 14.
  • 120 m 3 of cooling water per hour are guided in the cooler 17 via the lines 15 and 16.
  • B. could be the pre-cooler of a coking plant, heated there to 78 ° C and given via lines 18, 19, 20, 21 and 22 at 77 ° C to the head of the direct heat exchanger 9.
  • the cooling water is cooled to 50 ° C. by heating and saturating the air conducted in countercurrent and leaves the direct heat exchanger via lines 23 and 24.
  • the air laden with the stripped volatiles can e.g. B. ge in the underfiring of a coke oven or in the regeneration of an oxidative desulfurization.
  • the amount of heat required for heating and water vapor saturation can also be obtained elsewhere, such as. B. in the abortion of an ammonium sulfide circuit wash or in the washing oil cooling of a benzene factory.
  • the stripper drain can also be placed entirely or partially in a gas scrubber. Acid can be added beforehand through line 26 in order to bind the remaining volatile ammonia. In this example, 265 g of 78% sulfuric acid are added per m 3 .
  • the stripper drain must be cooled before being placed in a gas wash.
  • the cables and units used here should be thermally insulated in the hot areas.
  • Example 2 The same liquid as in Example 1 is fed via lines 1 and 27 into heat exchanger 28, where it flows from the stripper outlet, which is fed out again via lines 5 and 29 into heat exchanger 28 and via line 30, to 82 ° C is heated and enters the stripper 4 via the lines 31 and 3. Here it is stripped and heated to 85 ° C. It leaves the stripper with a residual concentration of 61 mg of volatile ammonia, under 1 mg of hydrogen sulfide and 8 mg of hydrocyanic acid per 1. In countercurrent, 5,000 m 3 i. N. Air of 20 ° C / h with blower 25 leads via lines 7 and 8 into the direct heat exchanger 9, which they pass through line 10 at 75 ° C. and steam leaves saturated.
  • the gas purification is operated in such a way that the water introduced into the process through coal moisture and formation water (approx. 14% based on the coal used) is not used for washing out ammonia, hydrogen sulfide and hydrocyanic acid or one or two of these substances ⁇ can.
  • the entire excess water of the process to which in addition to the previously mentioned waters, other waters, such as. B. steam condensates come, are stripped by the inventive method.
  • 25 m 3 of water to be cleaned are added to the head of the stripper 4 at 70 ° C. via lines 1 to 3.
  • the salary of the feed water is 4.1 g / 1 for volatile ammonia, 0.98 g / 1 for hydrogen sulfide and 80 mg / 1 for hydrocyanic acid.
  • the water flowing out of the stripper at 80 ° C. has a volatile ammonia content of 50 mg / 1, a hydrogen sulfide content of less than 1 mg / 1 and a hydrocyanic acid content of 20 mg / 1.
  • the outlet of the stripper 4 is led via the lines 5 and 33 into the line 22, in which the 120 m 3 of water coming from line 21 mixes and through which the combined water reaches the direct heat exchanger 9.
  • only part of the water to be discharged from the process can also be cleaned, while another part is also used in the gas scrubbing.
  • acid can be added to the heat exchanger circuit via line 51.
  • the water withdrawn from the heat exchanger circuit via line 24 can be used as wash water for gas cleaning.
  • Example 3 has great advantages over a conventional abortion operation. Firstly, about 3.65 are t steam / h is less consumed (if one indirect heat exchanger 45 with steam operates) ', at the same time a corresponding required for condensing and cooling the vapor amount of cooling water is saved, is on the other of no external water entered in the system in the form of steam condensate, so that correspondingly less waste water is obtained.
  • the loaded gas from line 14 can also be fed into the underfeed of coke ovens, the calculation shown above showing that compared to British Patent No. 1,181,587 significant progress is being made.
  • an outlet temperature of the stripper of 70 ° C. is given for a good stripping effect.
  • the above-mentioned 400,000 kJ must be provided at least per m 3 of water to be stripped, in total 10,000,000 kJ according to the example given here, while only 2,500,000 kJ additional energy in a mode of operation as described here must be used because the remaining necessary energy in the form of waste water is available free of charge.
  • the additional heat exchanger 36 can also be dispensed with entirely if the stripper 4 is operated at 75 ° C. and the gas to liquid ratio is increased to 400 to 1.
  • a coal liquefaction plant produces 50 m 3 of water per hour, which in addition to various organic impurities contain 10 g of hydrogen sulfide and 30 g of ammonia / 1.
  • This water is added via lines 1, 2 and 3 at 80 ° C. to the top of the stripper 4, from which it is cleaned with a residual content of 80 mg NH 1/1 and below 1 mg H 2 S 1 above the lines 5 and 6 expire.
  • the gas enters the stripper 4 through the lines 10 and 11, frees the countercurrent water from ammonia and hydrogen sulfide and reaches the gas scrubber 45 in a closed circuit via the insulated lines 12, 13, 41, 42 and 44 , in which it is freed of ammonia and hydrogen sulfide and cooled. From there, it is fed directly via line 38, blower 39 and lines 40 and 8 into the Meleyer 9 returned. This completes the cycle.
  • 290 m 3 of cooling water of 82 ° C. are added to the direct heat exchanger 9 per hour, which cool down to 61 ° C. and are fed into the cooler 17 via the lines 23, 34 and 16. There, the water is heated to 83 ° C. and returned to the direct heat exchanger 9 via lines 18 to 22.
  • This cooling water circuit can also be supplied with a stripper drain via line 33.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Industrial Gases (AREA)
  • Physical Water Treatments (AREA)

Abstract

Dans un procédé pour l'élimination des substances volatiles contenues dans l'eau produite par des procédés de valorisation du charbon, l'on chauffe du gaz dans un échangeur de chaleur direct (9), qui est ensuite saturé de vapeur et utilisé pour chasser les substances volatiles dans un stripper (4). Le liquide qui passe dans l'échangeur de chaleur direct est préchauffé dans un ou plusieurs échangeurs de chaleur indirects (17, 36), avec utilisation partielle ou totale de la chaleur ainsi dégagée.
PCT/EP1985/000297 1984-07-19 1985-06-19 Procede pour eliminer les substances volatiles contenues dans l'eau produite par des procedes de valorisation du charbon Ceased WO1986000920A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19843426562 DE3426562A1 (de) 1984-07-19 1984-07-19 Verfahren zur entfernung von fluechtigen inhaltsstoffen aus bei kohlenveredlungsprozessen anfallenden waessern
DEP3426562.7 1984-07-19

Publications (1)

Publication Number Publication Date
WO1986000920A1 true WO1986000920A1 (fr) 1986-02-13

Family

ID=6241005

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP1985/000297 Ceased WO1986000920A1 (fr) 1984-07-19 1985-06-19 Procede pour eliminer les substances volatiles contenues dans l'eau produite par des procedes de valorisation du charbon

Country Status (3)

Country Link
JP (1) JPS61502764A (fr)
DE (1) DE3426562A1 (fr)
WO (1) WO1986000920A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19600774A1 (de) * 1996-01-11 1997-07-17 Biotecon Ges Fuer Biotechnologische Entwicklung & Consulting Mbh Cyanidentfernung aus Prozeßwasser

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2142417C1 (ru) * 1999-03-16 1999-12-10 Ульяновский государственный технический университет Способ вакуумной деаэрации воды
RU2142418C1 (ru) * 1999-03-23 1999-12-10 Ульяновский государственный технический университет Способ термической деаэрации воды
RU2238908C1 (ru) * 2003-08-05 2004-10-27 Ульяновский государственный технический университет Способ термической деаэрации воды
RU2240290C1 (ru) * 2003-11-11 2004-11-20 Ульяновский государственный технический университет Вакуумная деаэрационная установка
RU2276104C2 (ru) * 2004-05-11 2006-05-10 Государственное образовательное учреждение высшего профессионального образования "Ульяновский государственный технический университет" Способ подготовки подпиточной воды теплосети
JP2006232904A (ja) * 2005-02-23 2006-09-07 Hitachi Ltd 石炭ガス化システムのガス精製方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1099501B (de) * 1958-04-25 1961-02-16 Hoechst Ag Verfahren und Vorrichtung zur Desorption beladener Absorptionsmittel
US3920419A (en) * 1974-04-10 1975-11-18 Republic Steel Corp Method of removing ammonia from ammonia containing liquor
EP0029536A1 (fr) * 1979-11-19 1981-06-03 Sterling Drug Inc. Procédé pour séparer et récupérer de l'ammoniac de solutions aqueuses
US4277311A (en) * 1976-06-14 1981-07-07 Bethlehem Steel Corporation Apparatus for distillation

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1444972A1 (de) * 1962-09-29 1969-02-06 Still Fa Carl Verfahren und Vorrichtung zur Vermeidung des Anfallens von freies Ammoniak und Phenole enthaltenden Abwaessern bei der Gewinnung von Gasen fuer Heizzwecke durch Trockendestillation oder Entgasung von Kohlen
US3754376A (en) * 1972-02-01 1973-08-28 Texaco Inc Inert gas stripping of contaminated water
DE2330888A1 (de) * 1973-07-04 1975-04-30 Texaco Development Corp Verfahren zur entfernung gasfoermiger verunreinigungen aus wasser
US4260462A (en) * 1978-05-26 1981-04-07 United States Steel Corporation Process for separating acid gases and ammonia from dilute aqueous solutions thereof

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1099501B (de) * 1958-04-25 1961-02-16 Hoechst Ag Verfahren und Vorrichtung zur Desorption beladener Absorptionsmittel
US3920419A (en) * 1974-04-10 1975-11-18 Republic Steel Corp Method of removing ammonia from ammonia containing liquor
US4277311A (en) * 1976-06-14 1981-07-07 Bethlehem Steel Corporation Apparatus for distillation
EP0029536A1 (fr) * 1979-11-19 1981-06-03 Sterling Drug Inc. Procédé pour séparer et récupérer de l'ammoniac de solutions aqueuses

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19600774A1 (de) * 1996-01-11 1997-07-17 Biotecon Ges Fuer Biotechnologische Entwicklung & Consulting Mbh Cyanidentfernung aus Prozeßwasser

Also Published As

Publication number Publication date
JPS61502764A (ja) 1986-11-27
DE3426562A1 (de) 1986-01-30

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