EP1819421A1 - Procede de separation de matieres solides de laveurs de gaz - Google Patents

Procede de separation de matieres solides de laveurs de gaz

Info

Publication number
EP1819421A1
EP1819421A1 EP04798089A EP04798089A EP1819421A1 EP 1819421 A1 EP1819421 A1 EP 1819421A1 EP 04798089 A EP04798089 A EP 04798089A EP 04798089 A EP04798089 A EP 04798089A EP 1819421 A1 EP1819421 A1 EP 1819421A1
Authority
EP
European Patent Office
Prior art keywords
solids
flocculant
separation
scrubber
process according
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Withdrawn
Application number
EP04798089A
Other languages
German (de)
English (en)
Inventor
Frank Seida
Peter Graf
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.)
Ineos Composites IP LLC
Original Assignee
Ashland Licensing and Intellectual Property LLC
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 Ashland Licensing and Intellectual Property LLC filed Critical Ashland Licensing and Intellectual Property LLC
Publication of EP1819421A1 publication Critical patent/EP1819421A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D51/00—Auxiliary pretreatment of gases or vapours to be cleaned
    • B01D51/02—Amassing the particles, e.g. by flocculation
    • 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
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
    • 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
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents

Definitions

  • the present invention relates to a process for separating solids from gas scrubbers.
  • dusts are also released in addition to the flue gas which is then usually deposited by means of dust separators or dust filters.
  • Such dust collectors or dust filters can basically be distinguished according to their used physical separation principles.
  • Known dust collectors are e.g. Mass force separators, wet scrubbers or so-called filtering separators, which have the filtering effect of e.g. use mineral fibers, stainless steel fibers, etc.
  • flue gas desulphurisation For power plants that burn fossil fuels for power generation, flue gas desulphurisation is required by law. There are a variety of methods for flue gas desulfurization known. By way of example, reference is made here to the lime washing process, a wet desulphurization process. Normally, two-stage scrubber systems with pre-scrubber and main scrubber are used in flue-gas desulphurisation.
  • the first scrubber stage the so-called pre-scrubber
  • the first scrubber stage is operated in the strongly acidic pH medium and serves to separate the elements of the 7th main group of the periodic system.
  • the hot flue gases are cooled in the pre-scrubber and separated the sau ⁇ ren components such as HF and HCl, since fluorine and chlorine in the main scrubber have a strong impairment of gypsum quality result.
  • a mist eliminator is provided between the pre-scrubber and the main scrubber to prevent droplet cracks in the main scrubber and thus to prevent the entry of fluoride and chloride.
  • nen As reasons for the increased entry of the finest dust particles in the pre-scrubber can be called nen:
  • the washed-out dust load which concentrates in the form of sludge in the pre-scrubber, can lead to a large number of problems.
  • the introduced dust particles tend to crust on the fins of the Tropfenab ⁇ separator, which is usually located between the pre- and main scrubber, and to narrow the flue gas path.
  • the immediate consequence of this is a differential pressure increase ⁇ P across the mist eliminator.
  • this object can be achieved by a process for separating solids, in particular for flue gas desulphurization plants, which has at least one absorption device which is arranged downstream of a solids deposition device, wherein the solid matter not separated off at the solids deposition device is added by means of addition at least one flocculant and / or flocculant and is deposited using a Trennvor ⁇ direction.
  • the inventive method for solids separation from scrubbers has at least one absorption device, preferably a Schwefeldioxidabsorpti ⁇ onsstrom, in particular for flue gas cleaning, which may include, for example, a pre-scrubber and main scrubber.
  • the absorption apparatus is particularly preferably a conventional flue gas desulfurization scrubber (abbreviated hereafter as REA scrubber).
  • This absorption device is nachgeord ⁇ net a Feststoffabscheidungsvortechnische, i.
  • a solids separation or dust separation Before the absorption device there is a solids separation or dust separation.
  • the solid-state separation apparatuses known in the art which can carry out a solid / gas separation, e.g. from flue gases or other exhaust air streams occurring in industrial processes, such as, for example, the known mass-flow separators cyclone or sedimentation and rotary flow chamber, wet scrubbers or also filtering separators.
  • electrostatic precipitators are preferably used for separating solids.
  • Fig. 1 The inventive method is exemplified in Fig. 1 in the form of a circuit diagram showing a conventional REA pre-scrubber (1) or a related Vorwascherniklauf.
  • This pre-scrubber cycle with the pre-scrubber (1) has a pressure discharge (2), which leads to the waste water tank (3) of the flue gas desulfurization system, as well as a Um ⁇ ⁇ lzpumpvortechnisch (4) this Vorwaschernikanks (radiator pumps).
  • a separating device (5) has been introduced into this discharge, which serves for the thickening of the derived suspension or the separation of the entrained solids.
  • the integration of the separating device (5) into the pre-scrubber circuit takes place, for example, in such a way that a partial flow (7) to the separating device (5) is controlled via a control valve (6) which controls the discharge of a partial flow from the pre-scrubber (1) to the REA wastewater treatment plant ) to be led.
  • the dosage of the flocculant takes place before entering the separation device by means of a metering device (8) in front of the separation device (5), which is particularly preferably a hydrocyclone according to the invention.
  • the fine fraction is separated in the overflow of the separator as a clear phase (9) or returned to the REA pre-scrubber (1), while the lower reaches of the separator (5) the separated coarse fraction (10) of übli ⁇ chsee subsequent sewage plant ( 11) feeds.
  • Cyclones are able to separate solid particles or liquid droplets with the help of centrifugal and gravitational force.
  • Cyclones for liquid systems are also referred to as hydrocyclones, their use for the impregnation of turbidity and for the separation of solids from sludge such as e.g. has been the state of the art for many years in the area of the gypsum suspension or sink-float treatment.
  • the dusts released during the combustion of fuels for example, which can not be separated by means of dust collectors or dust filters, such as the electrostatic precipitators commonly used, are the smallest particles of flue dust whose diameter is 90% less than 5 ⁇ m lie so that the material suspended in the pre-scrubber material is very finely dispersed, because almost 100% of the material has a Korn ⁇ size ⁇ 20 microns. Due to the too low mass would therefore in the Voreriescher ⁇ a FesWsüssigtrennung by means of hydrocyclone procedurally not possible.
  • flocculants When selecting the flocculants to be used, it should be taken into account that the coagulation or flocculation of the solid particles places very high demands on the flocculant to be employed, since the pH of the scrubber liquid in continuous operation is around the pH 0 and the flakes formed be subjected to extreme mechanical stress in the separation devices, especially in hydrocyclones. Furthermore, flocculation must form spontaneously in the flow of the separation device if no mixing or conditioning vessels are provided in the plant circuit, in order to minimize the investment costs for the plant and the process engineering effort.
  • Such flocculants are to be used, which cause an enlargement of the particles or of the flake to be separated to at least> 15 .mu.m and more preferably to at least> 20 .mu.m in the Lane ⁇ set separator, so that there is a safe FesWlligigtrennung guaranteed and the gas scrubber, in particular the pre-scrubber no differential pressure increase .DELTA.P is observed.
  • flocculants and / or flocculants are understood to mean all substances and / or agents which can influence particle particles in such a way that they aggregate into flocs and can be removed from the system.
  • Flocculants according to the invention are thus all compounds or compositions which are suitable for dissolving liquids, for example when clarifying liquids, in the thickening and dewatering of sludge, for example in the purification of industrial and municipal wastewaters, the treatment of drinking water, the extraction of rock salt, hard coal, kaolin and ores are used by flotation etc. and In many cases, they are also simply designated by the terms flocculants or sedimentation accelerators.
  • polymers of nonionic, anionic and particularly preferably cationic vinyl and / or acrylate polymers which are used as flocculants in wastewater treatment, ore and coal preparation and papermaking.
  • water-soluble, cationic polyelectrolytes which are used in large quantities in water treatment plants worldwide, in particular for improving the flocculation and dewatering of the resulting sewage sludge and are generally made of polymers of cationized acrylic acid derivatives, such as e.g. cationic acrylic acid or methacrylic acid esters or copolymers of these esters with acrylamide etc.
  • Cationic flocculants are preferably used in the process according to the invention.
  • Flocculants which are particularly preferably used for the process according to the invention are flocculants which are prepared by the preparation process described in DE 100 61 483 A1.
  • the water-in-water polymer dispersions described therein are hereby incorporated by reference into the description of the present invention.
  • Particularly advantageous for the process according to the invention are the water-in-water polymer dispersions obtainable according to DE 100 61 483 A1 and manufactured or sold by Stockhausen GmbH & Co. KG, Krefeld under the trade name PRAESTOL® E 150.
  • the Praestol ® E 150 flocculant of the company Stockhau ⁇ sen without costly solvents and metering in the process be integrated NEN kön ⁇ , so that hereby investments for dissolving and dosing redu ⁇ sheet to a minimum and the operational safety of operated plant can be greatly increased.
  • a partial stream is taken from the flow of pre-scrubber washing liquid and the separator, preferably a hydrocyclone is supplied.
  • the highly solids-depleted top of the hydrocyclone is returned to the scrubber cycle as a clear phase. This procedure ensures the thickening and level of the pre-scrubber.
  • the solids-enriched underflow of the hydrocyclone is fed to the classical route of the wastewater treatment plant.
  • the conventional slurry of the pre-scrubber is closed because the entire pre-scrubber household is controlled by the separator or the hydrocyclone plant.
  • the solids stock in the absorption device e.g. In the pre-scrubber throughout the Be ⁇ operating period ⁇ 2g, preferably ⁇ 1, 5 g and more preferably ⁇ 1 g of solid per liter prewash liquid can be maintained, this very low Feststoff ⁇ concentration can be maintained under all operating conditions.
  • the ⁇ P of the mist eliminator shows no increase in the selected operating periods.
  • incrustations on the droplet separator can be prevented or excluded. Due to the higher thickening and the associated greater acid capacity, in particular with regard to the HF concentration, a return solution of already formed incrustations is effected.
  • the hydrocyclone is particularly preferably used as a separation device in the process according to the invention, because this separation unit meets the requirements set in practice, e.g. in a conventional flue gas desulfurization plant is fair, since the separation efficiency can be adjusted via the supplied volume flow effectively to the current operating conditions.
  • the circulation rate determines the volume flow of the hydrocyclone feed.
  • the design of the recirculation quantity depends on the amount of solid introduced into the pre-scrubber, the given structural conditions of the pre-scrubber and the predominant use of the power plant block.
  • the volume split indicates in what ratio the hydrocyclone feed is divided into the upper and lower reaches. Basically, the volume split is determined by the lower and upper runners of the hydrocyclone.
  • the feed as a first step for the design of the separating device to be used is to be fixed as a function of the amount of solids introduced.
  • the process according to the invention for solids separation in particular for flue gas desulphurization plants with the separation apparatus used, must be considered in the overall process of the plant in which the process according to the invention is used for the separation of solids, because the wastewater is e.g. via the hydrocyclone inlet of the wastewater treatment plant.
  • a further advantage of the method according to the invention is that it requires no external energy, which would have to be supplied, for example, via pumps and auxiliary units, and also requires no complicated control or control technology, since the system regulates itself and adapts itself to the changing operating states.
  • the process according to the invention for the separation of solids was put into operation in one of the three flue gas desulphurization plants of a power plant of the E. ON power plant group.
  • the flue gas desulfurization plants used there work according to the lime absorption process and are designed in two stages, i. they have a pre-scrubber and a main scrubber.
  • Solid input amount of flue gas ⁇ Dust concentration after separation on the E-filter
  • the inventive method has been integrated into an existing flue gas desulphurisation plant, and the plant is running smoothly in continuous operation since commissioning.
  • the separation device used was a hydrocyclone plant or Mehrcyyklonan plant of the company Schauenburg (Mühlheim a.d. Ruhr, Germany), which has proven both in the experimental phase as well as in continuous operation as reliable and patisum nan meeting.
  • the integration of the hydrocyclone in the pressure line of the precleaner cycle was carried out in such a way that after a control valve via a pressure line, a partial flow of about 17 rrvVh was discharged and led to a multi-cyclone station.
  • this feed line a mixing section is used, this mixing section is used for metering the flocculant in the feed line of the hydrocyclone.
  • the uniform distribution of the flocculant is effected by the addition of dilution water into the mixing section.
  • the flocculant used was PRAESTOL® E 150, which was added by means of an automatic dosing pump.
  • the amount of flocculant added was of the order of about 100 g / h, with about 350 l / h of dilution water being used for mixing.
  • the amount of cooler liquid to the hydrocyclone was about 17 m 3 / h.
  • the hydrocyclone was designed to give a volume separation of 1/3: 2/3 parts. This has the procedural effect that about 13 m 3 / h returned with a solids content of ⁇ 1 g / l in the pre-scrubber over the cyclone overflow or about 4 m 3 with a solids content of about 19 g / l to wastewater over the cyclone underflow are discharged.
  • the slurry is about 75 kg / h (4 m 3 / h ⁇ about 19 g / l).
  • the method according to the invention was likewise put into operation with a hydrocyclone as separation unit and since then the method has been operating without any problems.
  • the amount of wastewater was reduced from 7 to 3 m 3 / h.
  • the amount of wastewater was reduced from 7 to 3 m 3 / h.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Treating Waste Gases (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)

Abstract

Procédé de séparation de matières solides de laveurs de gaz, en particulier pour des installations de désulfuration de gaz de fumée. Selon ledit procédé, au moins un dispositif d'absorption est monté en aval d'un dispositif de séparation de matières solides, et la charge de matières solides qui n'est pas séparée par le dispositif de séparation de matières solides est séparée par ajout d'au moins un floculant et / ou agent de floculation à l'aide d'un dispositif de séparation.
EP04798089A 2004-11-26 2004-11-26 Procede de separation de matieres solides de laveurs de gaz Withdrawn EP1819421A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2004/013422 WO2006056222A1 (fr) 2004-11-26 2004-11-26 Procede de separation de matieres solides de laveurs de gaz

Publications (1)

Publication Number Publication Date
EP1819421A1 true EP1819421A1 (fr) 2007-08-22

Family

ID=34959386

Family Applications (1)

Application Number Title Priority Date Filing Date
EP04798089A Withdrawn EP1819421A1 (fr) 2004-11-26 2004-11-26 Procede de separation de matieres solides de laveurs de gaz

Country Status (3)

Country Link
US (1) US7575625B2 (fr)
EP (1) EP1819421A1 (fr)
WO (1) WO2006056222A1 (fr)

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US7875103B2 (en) * 2006-04-26 2011-01-25 Mueller Environmental Designs, Inc. Sub-micron viscous impingement particle collection and hydraulic removal system
JP6023099B2 (ja) 2011-03-17 2016-11-09 エコラボ ユーエスエー インコーポレイティド 再循環する洗浄溶液から汚れを連続的又は断続的に除去するための組成物及び方法
CA2852606C (fr) 2011-10-19 2021-11-02 Ashland Licensing And Intellectual Property Llc Composition comprenant un tensioactif non ionique et un polymere ionique
AT512479B1 (de) * 2012-02-10 2013-11-15 Andritz Energy & Environment Gmbh Verfahren zur feinstoffreduktion im rea-gips
JP6135086B2 (ja) * 2012-10-05 2017-05-31 栗田工業株式会社 脱硫排水の処理方法
WO2015035681A1 (fr) * 2013-09-16 2015-03-19 大连海事大学 Dispositif et procédé pour traiter les eaux usées de désulfuration de navires
CN114269692A (zh) * 2019-06-28 2022-04-01 埃科莱布美国股份有限公司 再循环洗涤溶液
CN110787564B (zh) * 2019-10-21 2021-06-11 北京科技大学 一种石灰石煅烧工艺中联合处理废气与废水的系统和方法

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Also Published As

Publication number Publication date
WO2006056222A1 (fr) 2006-06-01
US20060112824A1 (en) 2006-06-01
US7575625B2 (en) 2009-08-18

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