WO2005051522A1 - Verfahren und anlage zur gasreinigung - Google Patents
Verfahren und anlage zur gasreinigung Download PDFInfo
- Publication number
- WO2005051522A1 WO2005051522A1 PCT/EP2004/010972 EP2004010972W WO2005051522A1 WO 2005051522 A1 WO2005051522 A1 WO 2005051522A1 EP 2004010972 W EP2004010972 W EP 2004010972W WO 2005051522 A1 WO2005051522 A1 WO 2005051522A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- liquid
- absorption tower
- sea water
- pipeline
- sump
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
Definitions
- the invention relates to a method and a system for separating sulfur dioxide from exhaust gas, the exhaust gas being charged with sea water in an absorption tower and the sea water loaded with sulfur compounds being drawn off from the liquid sump of the absorption tower and being charged with fresh sea water.
- the washing liquid requirement in the absorption zone is determined by the mass transfer between the gas phase and the liquid phase. Within the known measures, the smallest possible amount of washing liquid is used. In order to minimize the washing liquid requirement, a packed column is often used, which ensures a good mass transfer. If seawater is used as the washing liquid, the amount of bicarbonate available is also fixed for a given amount of washing liquid. Regularly extends only to the binding of a fraction of the absorbed S0 2 amount, while by far the greater part of the S0 2 amount is deducted as dissolved, unbound S0 2 with the washing liquid from the liquid sump of the absorption tower. The liquid is also - due to the large C0 2 partial pressure of the exhaust gas - CO 2 saturated.
- the aerated post-reaction basin must be designed for a residence time of 10 to 15 minutes so that the reactions can proceed completely Roblem is an odor that sometimes escapes in the area of the post-reaction basin. It is based on the fact that unbound S0 2 escapes from the liquid flowing into the post-reaction basin, which is drawn off from the liquid sump of the absorption tower. The unbound SO 2 can hardly be oxidized even by strong ventilation
- EP-A-0295908 describes a method for separating S0 2 from exhaust gases, wherein exhaust gas is subjected to sea water in an absorption tower and the liquid sump of the absorption tower is aerated, whereby bisulfites contained in the liquid are converted into bisulfates.
- the liquid is removed from the liquid sump withdrawn and further treated in a post-reaction basin, the liquid being partly returned to the absorption tower
- EP-B-0756890 also describes a process for separating S0 2 from exhaust gases, in comparison with EP-A-0295908 working with a smaller system and smaller amounts of air for the formation of sulfate.
- the exhaust gas in the absorption tower is subjected to sea water, the The amount is such that the bicarbonates contained in the seawater are sufficient for a stochiometric conversion of the absorbed sulfur dioxide into bisulfites.
- the liquid sump of the absorption tower is aerated and the bisulfites are converted into bisulfates, the bisulfate-containing liquid being drawn off from the liquid sump of the absorption tower and for the purpose of Sulphate formation and the pH adjustment in a post-reaction pool with fresh sea water is also applied.
- This application also describes the regulation to a pH of 4.0 - 5
- the invention has for its object to further develop the method described above so that the very expensive and large post-reaction basin can be dispensed with and odor pollution by released SO 2 is reliabl
- the invention achieves the object in that the bisulfate-containing liquid is drawn off from the liquid sump of the absorption tower and fresh sea water is applied in a pipeline for the purpose of sulfate formation and pH adjustment (neutralization).
- the invention is based on the finding that sulfate formation and pH - Setting is completed after a reaction time of 1 to 2 minutes.This depends on the quality of the seawater, the sulfur content in the gas and the reaction conditions in the liquid sump of the absorption tower.This means that the large and expensive post-reaction basin can be dispensed with.It can be advantageous to add the pipeline ventilated with oxygen or air to support the chemical reaction
- the length of the pipeline can be further reduced if mixing devices are used in the pipeline, which produce an optimal mixing by generating a corresponding flow
- a prerequisite for dispensing with the after-reaction tank is that the desulfurization products are oxidized in the liquid sump of the absorption tower, while at the same time the total amount of sea water supplied to the absorption tower is dimensioned such that the bicarbonate content is sufficient for a stoichiometric conversion of the absorbed sulfur dioxide into bisulfites and that one pH control in the liquid sump takes place Only through these measures together can the reaction time be reduced, whereby the post-reaction basin can be replaced by a pipeline
- the washing liquid supplied to the absorption zone of the washing tower is dimensioned without taking into account the chemical reactions described so that the absorption tower achieves a predetermined washing efficiency, which is defined as the ratio of the SO 2 starting concentration and the S0 2 starting concentration of the flue gas, preferably with an absorption tower worked, which has a built-in absorption zone and is designed for a large, surface-specific liquid throughput.
- a predetermined washing efficiency which is defined as the ratio of the SO 2 starting concentration and the S0 2 starting concentration of the flue gas
- an absorption tower worked which has a built-in absorption zone and is designed for a large, surface-specific liquid throughput.
- the washing liquid recirculation means that the amount of bicarbonate available in the absorption tower and the hydraulic load on the absorption zone of the tower can be set independently of one another. It is understood that in this mode of operation, an additional sea water stream supplied to the washing liquid sump entfallt
- the adjustment of the pH in the range of pH 4.0 to 5, preferably 4.15 and 4.5 ensures a maximum bisulfite concentration in the relatively small liquid partial stream from the Absorption tower and creates the conditions for rapid conversion to bisulfates Due to the strongly acidic environment, a high rate of oxidation is guaranteed, so that a short residence time of the liquid in the liquid sump of the absorption tower is sufficient.
- the amount required dwell time approx. 1 to 2.5 minutes Due to the optimal conditions (small liquid flow, higher oxidation speed), the oxidation in the wash liquid sump of the absorption tower can be realized with only a small amount of technical equipment. Due to the small liquid volume, relatively small quantities of oxidizing air can also be used
- Aeration of the pipeline can be advantageous if the complete oxidation of the bisulfites in bisulfates in the liquid sump of the washing tower has not been carried out
- the air flow used to ventilate the liquid sump is expediently cooled by injecting water before entering the washing liquid sump.
- the basic structure of the system shown in Fig. 1 includes an absorption tower (1) with a connected flue gas system (2), a sea water pumping station (3), a pipeline (4), sea water supply lines (5a, 5b) to the absorption tower (1) and the pipeline (4 ) and a ventilation device (7) connected to the liquid sump (6) of the absorption tower (1), consisting of an air compressor (8) and air lances (9) arranged in the liquid sump (6).
- the absorption tower (1) is designed as a countercurrent washer, with sea water
- the absorption zone (10) of the tower has no internals via one or more nozzle levels.
- the absorption zone (10) of the tower has no internals. Liquid flows from the liquid sump (6) of the absorption tower (1) into the pipeline (4).
- Treated waste water (12) is returned to the sea from the pipeline (4)
- the alkalinity of sea water which is usually given as HC0 3 , is used to bind and neutralize the amount of S0 2 absorbed from the exhaust gas.
- Standard sea water with a chlorine content of 19 g / kg has an HC0 3 content of 0.14 g / kg
- the bicarbonate content can be up to 0.32 g / kg (Arabian Gulf), the values given being mean values, of which considerable local deviations, for example in sea bays or near river estuaries , occurrence
- the exhaust gas is subjected to sea water in the absorption tower (1), the gaseous sulfur dioxide contained in the exhaust gas being physically absorbed in the sea water used as the washing liquid
- the total amount of sea water supplied to the absorption tower is such that the bicarbonates contained in the sea water are sufficient only for a stochiometric conversion of the absorbed sulfur dioxide into bisulfites.
- the liquid sump (6) of Absorption tower (1) is aerated, whereby the bisulfites are converted into bisulfates.
- the liquid sump (6) there is a partial reaction and oxidation, which is represented in simplified form by the following equation
- the bisulfate-containing liquid is drawn off from the liquid sump (6) of the absorption tower (1) and fresh sea water is applied to it for the purpose of sulfate formation and pH adjustment in the pipeline (4).
- the sulfate formation in the pipeline (4) can be simplified by the following equation are reproduced
- the amount of liquid withdrawn from the liquid sump (6) is, depending on the size of the system, in the range from 8,000 to 40,000 m 3 / h.
- the pipeline (4) is usually operated at flow rates of 1.5-3.5 m / s, so that the diameter is 1.2 to 6.2 m
- the pipeline length at the aforementioned flow rates is 20 m to 60 m
- a shortening of the pipeline length results when using appropriate mixing devices, e.g. static mixers in the form of baffles or stirrers
- the ventilation device (19) can be used for this It can also be the case that the amount of liquid required for gas scrubbing in the absorption zone is so large that when using sea water as washing liquid with the liquid feed (5a), excess stoichiometric amounts of bicarbonates are fed to the absorption tower (1) then when the S0 2 concentration in the exhaust gas stream is low and sea water with a high bicarbonate content is available.
- the invention teaches that to reduce a uberstochiometric bicarbonate amount, a liquid stream through a return line (14) from the liquid sump (6)
- the bicarbonate quantity available in the absorption tower (1) and the hydraulic loading of the absorption zone (10) of the tower can be adjusted independently of one another by means of the washing liquid recirculation.
- the fresh water metering by means of line (13) to the liquid sump (6) of the absorber tion tower (1) omitted
- the sulfate formation reaction already takes place in part in the liquid sump (6) of the absorption tower.
- the amount of bicarbonate available for the chemical reactions can be controlled become
- Both the seawater additive flow (13) and the liquid flow (14) returned from the liquid sump (6) to the absorption zone (10) can be regulated.
- the quantity is controlled as a function of the pH value of the liquid withdrawn from the liquid sump (6)
- a measuring and regulating device (15) with a measuring transducer (16) for the actual pH value detection is provided, as well as regulating devices (17) for the quantity control of the sea water additional flow and the liquid flow (14) returned from the liquid sump (6) to the absorption zone (10) )
- the pH value of the liquid drawn off from the liquid sump (6) of the absorption tower (1) is measured, and deviations in the measured values from a target value defined in the range from pH 4.15 to pH 4.5 are determined.
- the measured value deviations determine that of the liquid sump (6) supplied seawater flow (13) or from the liquid sump (6) into the absorption zone (10) ckselle liquid stream (14) is regulated in terms of quantity by the amount of pH-dependent control of the pH of the Flusstechnikssumpfes (6) in a narrow tolerance range between pH 4.15 and pH is kept constant 4.5
- a pH value between pH 6.0 and pH 7 is set in the pipeline (4) by adding fresh sea water.
- About 1/3 of the total sea water supplied to the system is for the washing tower (1) and about 2/3 for the Pipeline (4) Since the oxidation is laid in the washing liquid sump (6), it is possible to work with significantly smaller amounts of air compared to the prior art, in which the oxidation takes place in a post-reaction basin.
- the air flow used for ventilation is expediently cooled by water injection
- the ventilation device (7) comprises a shower (18) with quench water, sea water also being used as quench water
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA002512779A CA2512779A1 (en) | 2003-11-11 | 2004-10-01 | Method and installation for purifying gas |
US10/543,973 US7288235B2 (en) | 2003-11-11 | 2004-10-01 | Method and installation for purifying gas |
EP04790082A EP1682249A1 (de) | 2003-11-11 | 2004-10-01 | Verfahren und anlage zur gasreinigung |
NO20062064A NO20062064L (no) | 2003-11-11 | 2006-05-08 | Metode og installasjon for rensing av gass. |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10352638A DE10352638B4 (de) | 2003-11-11 | 2003-11-11 | Verfahren und Anlage zur Gasreinigung |
DE10352638.2 | 2003-11-11 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2005051522A1 true WO2005051522A1 (de) | 2005-06-09 |
Family
ID=34584979
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2004/010972 WO2005051522A1 (de) | 2003-11-11 | 2004-10-01 | Verfahren und anlage zur gasreinigung |
Country Status (9)
Country | Link |
---|---|
US (1) | US7288235B2 (de) |
EP (1) | EP1682249A1 (de) |
KR (1) | KR20060115572A (de) |
CN (1) | CN100336579C (de) |
CA (1) | CA2512779A1 (de) |
DE (1) | DE10352638B4 (de) |
NO (1) | NO20062064L (de) |
WO (1) | WO2005051522A1 (de) |
ZA (1) | ZA200505344B (de) |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1967253A1 (de) * | 2007-03-09 | 2008-09-10 | Enviroserv Gmbh | Waschturm |
US9757686B2 (en) | 2008-06-13 | 2017-09-12 | Sigan Peng | Ship flue gas scrubbing apparatus and method |
AU2008357629B2 (en) * | 2008-06-13 | 2015-09-03 | Sigan Peng | Washing device and washing method for marine exhaust flue gases |
AU2008357630B2 (en) * | 2008-06-13 | 2013-08-01 | Sigan Peng | Ship Flue Gas Desulphurization Method and Equipment |
AU2010325625A1 (en) * | 2009-12-02 | 2012-07-26 | Subrahmanyam Kumar | A process and system for quenching heat, scrubbing, cleaning and neutralizing acidic media present in the flue gas from the firing of fossil fuel |
CN102852596A (zh) * | 2011-07-01 | 2013-01-02 | 彭斯干 | 一种优化内燃机排气背压的方法、装置和系统 |
JP2013158720A (ja) * | 2012-02-06 | 2013-08-19 | Mitsubishi Heavy Ind Ltd | 脱硫海水処理システム |
EP2738364A1 (de) | 2012-11-29 | 2014-06-04 | Alfa Laval Corporate AB | Abgaswäscher, System zur Behandlung der Waschflüssigkeit und Verwendung eines Abgaswäschers |
KR101422760B1 (ko) * | 2014-03-06 | 2014-07-23 | (주) 한국환경진단연구소 | 해수를 이용하여 배가스에 포함된 황 화합물을 제거하는 장치 및 방법 |
JP6285773B2 (ja) * | 2014-03-28 | 2018-02-28 | 富士電機株式会社 | 排ガス処理装置の排水処理方法 |
CN111807495A (zh) * | 2020-08-05 | 2020-10-23 | 西安热工研究院有限公司 | 一种防止间接空冷循环水系统腐蚀的水质控制装置及方法 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4085194A (en) * | 1972-05-08 | 1978-04-18 | Hitachi, Ltd. | Waste flue gas desulfurizing method |
DE19535475C1 (de) * | 1995-09-23 | 1997-04-10 | Lentjes Bischoff Gmbh | Verfahren zum Abtrennen von Schwefeldioxid aus Abgas |
DE19815207C1 (de) * | 1998-04-04 | 1999-06-24 | Steinmueller Gmbh L & C | Verfahren zum Abtrennen von Schwefeldioxid aus Abgas mittels Meerwasser und Rauchgasentschwefelungsanlage zur Durchführung des Verfahrens |
DE19752470A1 (de) * | 1997-11-27 | 1999-06-24 | Lurgi Lentjes Bischoff Gmbh | Verfahren und Anlage zum Abtennen von SO¶2¶ aus Abgas |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
NO156235C (no) * | 1980-02-13 | 1988-02-02 | Flaekt Ab | Fremgangsmaate ved absorpsjon av svoveloksyder fra roekgasser i sjoevann. |
US4804523A (en) * | 1987-06-17 | 1989-02-14 | Bechtel Group, Incorporated | Use of seawater in flue gas desulfurization |
US5141727A (en) * | 1991-06-03 | 1992-08-25 | Varney John W | Flue gas treatment |
DE19527836A1 (de) * | 1995-07-29 | 1997-01-30 | Gottfried Bischoff Gmbh & Co | Verfahren zum Abtrennen von Schwefeldioxid aus Abgas |
DE29517697U1 (de) | 1995-07-29 | 1996-01-18 | Gottfried Bischoff GmbH & Co. KG, 45136 Essen | Rauchgasentschwefelungsanlage |
DE19746337B4 (de) * | 1997-10-21 | 2005-06-09 | Centrotherm Abgastechnik Gmbh | Vorrichtung zum Neutralisieren von Kondensat aus dem Abgas einer Verbrennungseinrichtung |
CN1262145A (zh) * | 1999-01-26 | 2000-08-09 | 彭斯干 | 纯海水工业烟气脱硫方法 |
JP2001129352A (ja) * | 1999-11-02 | 2001-05-15 | Fujikasui Engineering Co Ltd | 海水による排ガス脱硫高度処理プロセス |
CN2570255Y (zh) * | 2002-09-20 | 2003-09-03 | 青岛海洋大学 | 一种海水脱硫用的综合处理装置 |
-
2003
- 2003-11-11 DE DE10352638A patent/DE10352638B4/de not_active Expired - Fee Related
-
2004
- 2004-10-01 EP EP04790082A patent/EP1682249A1/de not_active Withdrawn
- 2004-10-01 KR KR1020057013143A patent/KR20060115572A/ko not_active Application Discontinuation
- 2004-10-01 US US10/543,973 patent/US7288235B2/en not_active Expired - Fee Related
- 2004-10-01 CA CA002512779A patent/CA2512779A1/en not_active Abandoned
- 2004-10-01 WO PCT/EP2004/010972 patent/WO2005051522A1/de active Application Filing
- 2004-10-01 CN CNB2004800029837A patent/CN100336579C/zh not_active Expired - Fee Related
-
2005
- 2005-07-01 ZA ZA200505344A patent/ZA200505344B/en unknown
-
2006
- 2006-05-08 NO NO20062064A patent/NO20062064L/no not_active Application Discontinuation
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4085194A (en) * | 1972-05-08 | 1978-04-18 | Hitachi, Ltd. | Waste flue gas desulfurizing method |
DE19535475C1 (de) * | 1995-09-23 | 1997-04-10 | Lentjes Bischoff Gmbh | Verfahren zum Abtrennen von Schwefeldioxid aus Abgas |
DE19752470A1 (de) * | 1997-11-27 | 1999-06-24 | Lurgi Lentjes Bischoff Gmbh | Verfahren und Anlage zum Abtennen von SO¶2¶ aus Abgas |
DE19815207C1 (de) * | 1998-04-04 | 1999-06-24 | Steinmueller Gmbh L & C | Verfahren zum Abtrennen von Schwefeldioxid aus Abgas mittels Meerwasser und Rauchgasentschwefelungsanlage zur Durchführung des Verfahrens |
Also Published As
Publication number | Publication date |
---|---|
CN1744938A (zh) | 2006-03-08 |
CA2512779A1 (en) | 2005-06-09 |
CN100336579C (zh) | 2007-09-12 |
ZA200505344B (en) | 2006-04-26 |
EP1682249A1 (de) | 2006-07-26 |
NO20062064L (no) | 2006-07-11 |
DE10352638A1 (de) | 2005-06-16 |
US7288235B2 (en) | 2007-10-30 |
DE10352638B4 (de) | 2007-10-11 |
KR20060115572A (ko) | 2006-11-09 |
US20060251559A1 (en) | 2006-11-09 |
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