DK170605B1 - Process for cleaning off exhaust gas - Google Patents
Process for cleaning off exhaust gas Download PDFInfo
- Publication number
- DK170605B1 DK170605B1 DK513988A DK513988A DK170605B1 DK 170605 B1 DK170605 B1 DK 170605B1 DK 513988 A DK513988 A DK 513988A DK 513988 A DK513988 A DK 513988A DK 170605 B1 DK170605 B1 DK 170605B1
- Authority
- DK
- Denmark
- Prior art keywords
- exhaust gas
- slurry
- water
- alkaline earth
- ash
- 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
- B01D53/14—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
-
- 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
Landscapes
- 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)
- Processing Of Solid Wastes (AREA)
Description
i DK 170605 B1in DK 170605 B1
Den foreliggende opfindelse angår en fremgangsmåde til behandling af afgangsgas indeholdende urenheder omfattende et eller flere sure oxider af svovl, nitrogen, carbon og halogen og sure halogenforbindelser, hvilken afgangs-5 gas har en temperatur, der er større end gassens fortætningspunkt, hvorved afgangsgassen bringes i kontakt med vand og aske indeholdende alkalimetalforbindelser, fortrinsvis natrium- og kaliumforbindelser, og jordalkalime-talforbindelser, således at afgangsgassen vaskes og 10 syrerne, som er dannet ved de i afgangsgassen indeholdte urenheders kontakt med opslæmningens vand, omsættes med oxider, hydroxider og carbonater af alkali- og jordalka-limetallet i opløsningen, hvorved der dannes en opløsning indeholdende opløste alkali- og jordalkalimetalsalte og 15 et bundfald af uopløselige alkali- og jordalkalimetalsalte.The present invention relates to a process for treating exhaust gas containing impurities comprising one or more acid oxides of sulfur, nitrogen, carbon and halogen and acidic halogen compounds, which exhaust gas has a temperature greater than the gas condensation point, whereby the exhaust gas is introduced into the gas. contact with water and ash containing alkali metal compounds, preferably sodium and potassium compounds, and alkaline earth metal compounds, so that the exhaust gas is washed and the acids formed by the contact of the slurry's impurities with the slurry's water are reacted with oxides, hydroxides and carbonates and the alkaline earth metal in the solution, forming a solution containing dissolved alkali and alkaline earth metal salts and a precipitate of insoluble alkali and alkaline earth metal salts.
Bortrensning af urenheder i afgangsgas er generelt dyr, idet der opnås væsentlige miljømæssige men kun få eller 20 slet ingen økonomiske fordele, medmindre det ved rensningen er muligt at omdanne materialer, der ellers ville være spildmaterialer, til nyttige produkter. Anlægsomkostningerne er store. Endvidere udgør de til rensningen anvendte materialer, f.eks. oxider, carbonater og hydroxid-25 er af alkali- og eller jordalkalimetaller, en yderligere omkostning, ligesom deponering af reaktionsprodukterne, især hvis disse indeholder giftige komponenter, fra reaktionen mellem rensningsmaterialer og afgangsgas yderligere forøger omkostningerne.Waste gas purification is generally expensive, with significant environmental benefits but few or no economic benefits, unless it is possible to purify materials which would otherwise be wasteful materials into useful products. Construction costs are high. Furthermore, the materials used for purification, e.g. oxides, carbonates and hydroxides of alkali and or alkaline earth metals, an additional cost, as does the deposition of the reaction products, especially if they contain toxic components, from the reaction between purification materials and waste gas further increases the cost.
3030
Et stigende antal kedelanlæg fyres ved forbrænding af biologiske materialer (i det følgende kollektivt betegnet "biomasse") herunder træ, tørv eller rester fra afgrøder.An increasing number of boiler plants are fired by the burning of biological materials (hereinafter collectively referred to as "biomass") including wood, peat or crop residues.
I disse anlæg produceres kun få eller ingen svovloxider, 35 og der kræves og foretages derfor ingen rensning af de gasformige komponenter i afgangsgassen. På den anden side indeholder den i sådanne anlæg producerede aske væsentli DK 170605 B1 2 ge mængder alkali- og jordalkalimetalsalte, der sædvanligvis forekommer som oxider eller, hvis de er befugtede og/eller reageret med carbondioxid, som hydroxider eller carbonater, eventuelt som hydratiserede salte.In these plants, only few or no sulfur oxides are produced, 35 and therefore no purification of the gaseous components of the exhaust gas is required and performed. On the other hand, the ash produced in such plants contains substantially quantities of alkali and alkaline earth metal salts which usually appear as oxides or, if moistened and / or reacted with carbon dioxide, as hydroxides or carbonates, optionally as hydrated salts .
55
Det har vist sig, at aske fra kedelanlæg, hvor alkali- og jordalkalimetaloxider, -hydroxider og/eller -carbonater udgør en væsentlig del af asken, kan anvendes i stedet for ovennævnte sædvanlige materialer til rensning af af-10 gangsgas, hvorved et produkt, der ellers ville være et spildprodukt, kan anvendes til erstatning for materialer, der er dyre i indkøb.It has been found that ash from boiler plants where alkali and alkaline earth metal oxides, hydroxides and / or carbonates constitute a substantial part of the ash can be used in place of the above-mentioned usual materials for purifying waste gas, whereby a product, that would otherwise be a waste product can be used to replace materials that are expensive to purchase.
På tale som anvendelige materialer kommer aske fra for-15 brændingsanlæg for industrielt eller kommunalt affald, indeholdende kalium eller natrium eller andre opløselige salte, der ved opløsning i vand danner en basisk opløsning (med stor pH-værdi) og efter genindvinding fra opløsningen tilvejebringer en økonomisk fordel.As useful materials, ash comes from industrial or municipal waste incinerators containing potassium or sodium or other soluble salts which, when dissolved in water, form a basic solution (of high pH) and after recovery from the solution provide a economical benefit.
20 I det følgende betegnes den ved den her omhandlede fremgangsmåde anvendelige aske, der fremkommer ved brænding af biomasse og industrielle eller kommunale spild- eller andre biprodukter, med den generiske term "aske".20 In the following, the ash applicable to this process, which arises from the burning of biomass and industrial or municipal waste or other by-products, is referred to by the generic term "ash".
2525
Desværre skal den uopløselige del af reageret aske sædvanligvis stadig fjernes som spildprodukt, f.eks. er den uanvendelig til andet brug i forbindelse med de fleste kedelanvendelsesmuligheder. Spildproduktet er imidlertid 30 ikke længere et basisk materiale og kan i de fleste tilfælde deponeres som benignt almindeligt fyldmateriale el- ^ ler i visse landfyldninger anvendes som dækmateriale.Unfortunately, the insoluble portion of reacted ash is usually still removed as a waste product, e.g. it is unusable for other use in connection with most boiler applications. However, the waste product is no longer a basic material and can in most cases be deposited as benign ordinary filler material or in some land fillings used as cover material.
Hvis spildproduktsammensætningen og transportomkostnin-gerne tillader det, er dette produkt endvidere anvende-35 ligt som udgangsmateriale i cementovne. I visse andre situationer, som ved den her omhandlede fremgangsmåde, er den uopløselige del af rensematerialet anvendeligt til DK 170605 B1 3 fremstilling af calciumsulfat eller gips eller som mineralfyldstof.Furthermore, if the waste product composition and transport costs allow, this product is useful as a starting material in cement kilns. In certain other situations, as in the present process, the insoluble portion of the cleaning material is useful for the preparation of calcium sulphate or gypsum or as mineral filler.
Hvis det anlæg, der producerer asken, ikke selv har en 5 kedel, der producerer en afgangsgas med stort svovlindhold, som skal renses, kan asken transporteres til andre kedelanlæg, der måtte have et sådant problem eller til anlæg, hvor anvendelse af et brændstof med højere svovlindhold kunne frembyde en økonomisk fordel. Da aske fra 10 biomassemateriale i almindelighed indeholder kalium og andre alkali- og jordalkalimetalsalte, der kan genindvindes under anvendelse af varmen fra afgangsgassen eller andre spildmateriale, kan de resulterende alkali- eller jordalkalimetalsalte udgøre et værdifuldt bi-produkt ved 15 processen.If the ash-producing plant does not itself have a boiler producing a high sulfur content of exhaust gas to be purified, the ash may be transported to other boiler plants which may have such a problem or to plants using a fuel with higher sulfur content could offer an economic advantage. Since ash from 10 biomass material generally contains potassium and other alkali and alkaline earth metal salts which can be recovered using the heat of the exhaust gas or other waste material, the resulting alkali or alkaline earth metal salts may constitute a valuable by-product of the process.
Ifølge opfindelsen tilvejebringes en hidtil ukendt fremgangsmåde til rensning af afgangsgas, hvilken fremgangsmåde er af den i krav l's indledning anførte art, og som 20 er ejendommelig ved det i krav l's kendetegnende del angivne .According to the invention, there is provided a novel process for purifying exhaust gas, which is of the kind set forth in the preamble of claim 1 and which is peculiar to the characterizing part of claim 1.
De for tiden foretrukne fremgangsmåder omfatter et eller flere af følgende trin: strømmen af afgangsgas bringes i 25 kontakt med opslæmningen, idet strømmen føres gennem op slæmningen, opløsningen af alkali- og jordalkalimetalsalte separeres fra det udfældede materiale og uopløste bestanddele; opløsningen af alkali- og jordalkalimetalsalte samt det udfældede materiale og de uopløste komponenter 30 overføres til et separationssystem, i hvilket saltopløsningen separeres fra det udfældede materiale og de uopløste komponenter; den separerede saltopløsning føres gennem en varmeveksler, hvor opløsningen udtrækker varme fra strømmen af afgangsgas, inden denne bringes i kontakt 35 med opslæmningen; strømmen af afgangsgas afkøles til af-fugtning af denne inden kontakttrinnet; saltopløsningen anvendes til afkøling og affugtning af strømmen af af- 4 DK 170605 B1 gangsgas; varmen fra strømmen af afgangsgas anvendes til fjernelse af vand fra saltopløsningen, idet varmen delvis skaffes fra en eller flere af følgende kilder: (A) den varme afgangsgas, (B) den latente fordampningsvarme fra 5 eventuel fugt i strømmen af afgangsgas, (C) hydratise- ringsreaktionen mellem aske og vand, og (D) kompression * af gassen inden kontakttrinnet.The presently preferred methods comprise one or more of the following steps: the effluent gas stream is contacted with the slurry, the stream being passed through the slurry, the solution of alkali and alkaline earth metal salts separated from the precipitated material and undissolved constituents; the solution of alkali and alkaline earth metal salts as well as the precipitated material and the undissolved components 30 is transferred to a separation system in which the saline solution is separated from the precipitated material and the undissolved components; the separated saline solution is passed through a heat exchanger where the solution extracts heat from the exhaust gas stream before contacting it with the slurry; the exhaust gas stream is cooled to dehumidify it before the contact step; the saline solution is used to cool and dehumidify the flow of the exhaust gas; the heat from the waste gas stream is used to remove water from the brine solution, the heat being partially obtained from one or more of the following sources: (A) the hot exhaust gas, (B) the latent evaporative heat from any moisture in the exhaust gas stream, (C) the hydration reaction between ash and water; and (D) compression * of the gas prior to the contact step.
I det følgende beskrives opfindelsen nærmere under hen-10 visning til tegningen, som skematisk viser et anlæg til udøvelse af den her omhandlede fremgangsmåde.The invention will now be described in more detail with reference to the accompanying drawing, which schematically illustrates an apparatus for carrying out the method of the present invention.
Som vist pumpes en opslæmning, som ved positionen 8 kommer fra en (ikke vist) aske/vand-blandetank, via et rør 15 10 ind i en behandlingstank 12 sammen med supplerende vand, der indføres via en indgang 14 fra en passende (ikke vist) kilde. Herved fremstilles en fortyndet opslæmning 16. Asken køres ind fra en kilde, f.eks. et genereringsanlæg, der fyres med biomasse, eller et forbræn-20 dingsanlæg, der fyres med spildmateriale. Afgangsgas fra en cementovn, et forbrændingsanlæg eller en kedel (ikke vist) indeholdende et eller flere oxider af svovl, nitrogen, carbon og/eller halogenforbindelser, herunder halogenoxider, går ind i en varmeveksler 22 via en indgang 25 18, og den udgår som en afkølet afgangsgas. Kondenseret vand fra afgangsgassen opsamles i en varmeveksler 22 og overføres til behandlingstanken 12 via et rør 44. Afgangsgassen bevæger sig derpå videre til en kompressor 20 via et rør 23, og via et rør 24 overføres den til forde-30 lingsrør 26, der er anbragt ved bunden af behandlingstanken 12. For at undgå udfældning af fast materiale på bun-den af behandlingstanken 12, kan opslæmningen omrøres eller recirkuleres ved hjælp af passende organer, f.eks. en recirkulationspumpe 27.As shown, a slurry, which at position 8 comes from a (not shown) ash / water mixing tank, is pumped into a treatment tank 12 via a pipe 15 10 along with supplemental water fed through an inlet 14 from a suitable (not shown) ) source. This produces a diluted slurry 16. The ash is run from a source, e.g. a generating plant fired with biomass, or a combustion plant fired with waste material. Exhaust gas from a cement furnace, incinerator or boiler (not shown) containing one or more oxides of sulfur, nitrogen, carbon and / or halogen compounds, including halogen oxides, enters a heat exchanger 22 via an inlet 25 18 and it exits as a cooled exhaust gas. Condensed water from the exhaust gas is collected in a heat exchanger 22 and transferred to the treatment tank 12 via a pipe 44. The exhaust gas then moves on to a compressor 20 via a pipe 23 and via a pipe 24 it is transferred to distribution pipe 26 which is arranged. at the bottom of the treatment tank 12. In order to avoid precipitation of solid material at the bottom of the treatment tank 12, the slurry may be stirred or recycled by means of suitable means, e.g. a recirculation pump 27.
Afgangsgassen bobler gennem opslæmningen 16 af aske og vand og passerer ud gennem tankens Øvre del som renset 35 DK 170605 B1 5 afgangsgas 28. Opslæmningen 16, der er en blanding af behandlet fast materiale, vand og opløste materialer, pumpes med en pumpe 32 via et rør 30 til en udfældningstank 34, hvor det udfældede faste materiale 36 pumpes ud med 5 en pumpe 38, medens vandet 37, som indeholder opløste salte, pumpes til varmeveksleren 22, hvor det afkøler den indførte afgangsgas. Vandet fra saltopløsningen 37 afdampes og udføres til atmosfæren via et rør 40, men vandet kan også afdampes og derpå kondenseres til en væske, så-10 ledes at man genvinder den latente varme, som kan genanvendes. Saltene fra saltopløsningen 37 koncentreres og/eller udfældes og udtages fra varmeveksleren via et rør 42. De kationiske komponenter i de udtagne salte er i hovedsagen calcium, kalium, magnesium og natrium. De an-15 ioniske komponenter i saltene er i hovedsagen sulfat, carbonat og nitrat. Den aktuelle sammensætning af saltene vil afhænge af den oprindelige sammensætning af den aske, som behandles, samt af sammensætningen af afgangsgassen.The exhaust gas bubbles through the ash and water slurry 16 and passes out through the upper portion of the tank as purified exhaust gas 28. The slurry 16, which is a mixture of treated solid, water and dissolved materials, is pumped with a pump 32 via a pipe 30 to a precipitation tank 34, where the precipitated solid 36 is pumped out with 5 a pump 38, while the water 37 containing dissolved salts is pumped to the heat exchanger 22 where it cools the introduced exhaust gas. The water from the saline solution 37 is evaporated and discharged to the atmosphere via a pipe 40, but the water can also be evaporated and then condensed into a liquid to recover the latent heat which can be reused. The salts from the brine 37 are concentrated and / or precipitated and removed from the heat exchanger via a tube 42. The cationic components of the salts taken out are mainly calcium, potassium, magnesium and sodium. The anionic components of the salts are mainly sulfate, carbonate and nitrate. The actual composition of the salts will depend on the initial composition of the ash being treated as well as the composition of the exhaust gas.
20 Aske fra biomasse-forbrændingssystemer kan indeholde uforbrændt carbon, eventuelt flydende i vand. Den her omhandlede proces kan om ønsket modificeres som vist i figuren til fjernelse af carbon. Vandet 37 Indeholdende uforbrændt carbon pumpes fra udfældningstankens overflade 25 til filtrering eller anden behandling til fjernelse af carbon, og genindføres derefter i processen. Om nødvendigt kan opløsningen indeholdende opløste alkali- og jordalkalimetalsalte fjernes gennem et ledningssystem (ikke vist) til bortfiltrering eller anden bortrensning 30 af partikelformigt materiale i et apparat til fjernelse af sådant materiale. Opløsningen ledes derefter til varmeveksleren 22.20 Ashes from biomass combustion systems may contain unburnt carbon, possibly floating in water. The process of the present invention can be modified as desired in the figure for removing carbon. The water 37 Containing unburnt carbon is pumped from the precipitation tank surface 25 for filtration or other treatment to remove carbon, and then reintroduced in the process. If necessary, the solution containing dissolved alkali and alkaline earth metal salts can be removed through a conduit system (not shown) for filtration or other purification of particulate material in an apparatus for removing such material. The solution is then passed to the heat exchanger 22.
Den kendte varmeveksler 22 tjener både som varmeveksler-35 og krystallisationsenhed. Den udtrækker varme fra afgangsgassen og anvender denne varme, herunder latent varme fra kondenseringen af vandet i afgangsgassen, til af- 6 DK 170605 dampning af vand.The known heat exchanger 22 serves as both heat exchanger 35 and crystallization unit. It extracts heat from the exhaust gas and uses this heat, including latent heat from the condensation of the water in the exhaust gas, to evaporate water.
Hele systemet er sammensat af velkendte dele, der er kombineret under anvendelse af kendt teknik. F.eks. kan 5 behandlingstanken typisk have et volumen på 3.800.000 1 og være forsynet med organer til omrøring og gasforde- ; ling. Udfældningstanken han have et volumen på 380.000 1.The entire system is composed of well known parts which are combined using prior art. For example. the treatment tank may typically have a volume of 3,800,000 liters and be provided with stirring and gas distribution means; Ling. The precipitation tank he has a volume of 380,000 1.
Begge tanke kan være konstrueret af rustfrit stål eller andet egnet materiale, f.eks. gummi, der kan tåle stærkt 10 alkaliske eller sure opløsninger.Both tanks may be constructed of stainless steel or other suitable material, e.g. rubber that can withstand highly alkaline or acidic solutions.
Det fundamentale funktionsprincip ved opfindelsen er forening og omsætning af to strømme af spildmateriale, der er fremstillet under brændeprocessen, til tilvejebringel-15 se af gensidig neutralisation af spildmaterialerne. Den ene strøm af spildmateriale er de gasser og gasformige oxider, der danner sure vandige opløsninger, og den anden det partikelformige materiale, nemlig aske fra et forbrændingsanlæg, der fyres med biomasse eller industrielt 20 eller kommunalt affald, der fører til dannelse af basiske vandige opløsninger.The basic principle of operation of the invention is the unification and conversion of two streams of waste material produced during the firing process to provide mutual neutralization of the waste materials. One stream of waste material is the gases and gaseous oxides that form acidic aqueous solutions, and the other the particulate material, namely ash from a biomass or industrial waste or municipal waste incineration plant leading to the formation of basic aqueous solutions. .
Efter delvis opløsning i vand reagerer de to spildmaterialer indbyrdes under gensidig neutralisation. Når der 25 er tale om aske, åbner processen mulighed for reaktion eller fjernelse af de basiske komponenter. Det herved dannede neutrale faste materiale er derpå egnet til deponering som ufarligt spildprodukt. Samtidig renses den gennem opslæmningen i behandlingstanken gående afgangsgas 30 for en betydelig andel af halogenforbindelserne samt svovl-, nitrogen- og halogenoxiderne, idet der dannes salte af disse komponenter.After partial dissolution in water, the two wastes react with each other under mutual neutralization. In the case of ash, the process allows for the reaction or removal of the basic components. The neutral solid thus formed is then suitable for disposal as a non-hazardous waste product. At the same time, the exhaust gas 30 passing through the slurry in the treatment tank is purified for a significant proportion of the halogen compounds as well as the sulfur, nitrogen and halogen oxides, forming salts of these components.
35 DK 170605 B1 735 DK 170605 B1 7
EKSEMPELEXAMPLE
Afgangsgas f.eks. fra en kedel føres via en ledning 18 ind i varmeveksleren 22 ved hjælp af kompressoren 20 med 3 5 en hastighed på 6000 m /min. Afgangsgassen har en variabel sammensætning, men indeholder omtrent 10% vand, 15% carbondioxid, 65% nitrogen, 10% oxygen og 500-1000 dpm nitrogenoxid og 100-1000 dpm svovldioxid. I varmeveksleren 22 afkøles afgangsgassen, og der udkondenseres vand, 10 hvilket fører til en strømningsvolumenformindskelse. Derefter udtages afgangsgassen med kompressoren 20 via et rør 23, idet den føres frem til fordelingsrørene 26 via røret 24, hvorefter den reagerer med opslæmningen 16, hvor halogenforbindelser, svovl-, nitrogen- carbon- og 15 halogenoxider omsættes.Exhaust gas e.g. from a boiler, via a line 18 is fed into the heat exchanger 22 by means of the compressor 20 at a speed of 6000 m / min. The exhaust gas has a variable composition but contains about 10% water, 15% carbon dioxide, 65% nitrogen, 10% oxygen and 500-1000 ppm nitric oxide and 100-1000 ppm sulfur dioxide. In the heat exchanger 22, the exhaust gas is cooled and water is condensed, 10 leading to a flow volume decrease. Then, the exhaust gas with the compressor 20 is taken out via a pipe 23, which is advanced to the distribution pipes 26 via the pipe 24, after which it reacts with the slurry 16, where halogen compounds, sulfur, nitrogen carbon and halogen oxides are reacted.
Asken indføres i behandlingstanken 12 med en hastighed på 7200-10.800 kg per h (tørvægt). Der tilsættes vand, således at der fås en fortyndet opslæmning indeholdende op 20 til 95% vand. Opslæmningens vandindhold bestemmes af begyndelseskoncentrationen af alkali- og jordalkalimetal-salte eller andre metalsalte i asken og af den ønskede koncentration af disse salte i det resterende materiale.The ash is introduced into the treatment tank 12 at a rate of 7200-10,800 kg per h (dry weight). Water is added so that a diluted slurry containing up to 20 to 95% water is obtained. The water content of the slurry is determined by the initial concentration of alkali and alkaline earth metal salts or other metal salts in the ash and by the desired concentration of these salts in the remaining material.
25 Efter reaktion med afgangsgassen pumpes opslæmningen af den behandlede aske til udfældningstanken 34 med en hastighed på ca. 760 1/min. I denne tank udfældes det faste materiale under dannelse af en opslæmning bestående af ca. 35% vand og 65% fast materiale under en vandig opløs-30 ning af de under behandlingen opløste opløselige salte.After reaction with the exhaust gas, the slurry of the treated ash is pumped to the precipitation tank 34 at a rate of approx. 760 rpm In this tank, the solid material is precipitated to form a slurry consisting of ca. 35% water and 65% solid material under an aqueous solution of the soluble salts dissolved during the treatment.
Den vandige opløsning pumpes via udgangen 37 til varmeveksleren 22 med en hastighed på ca. 760 1/min, hvor den anvendes til afkøling af afgangsgassen, idet der afdampes vand fra opløsningen under dannelse af salte som bipro-35 dukt. Eventuelt svømmende carbon kan fjernes som ovenfor beskrevet. Biprodukterne i form af salte, som fjernes via røret 43, fremstilles i en mængde på ca. 5-20 ton pr dag 8 DK 170605 B1 og omfatter kaliumsulfat, kalciumcarbonat og andre salte med kationiske komponenter herunder kalium, calcium, magnesium og natrium samt anioniske komponenter omfattende carbonat, sulfat og nitrat. En del af nitratet oxiderer 5 sulfit til sulfat.The aqueous solution is pumped via the outlet 37 to the heat exchanger 22 at a rate of approx. 760 l / min, where it is used to cool the exhaust gas, evaporating water from the solution to form salts as a by-product. Any swimming carbon may be removed as described above. The by-products in the form of salts which are removed via the tube 43 are prepared in an amount of approx. 5-20 tonnes per day 8 and includes potassium sulphate, calcium carbonate and other salts with cationic components including potassium, calcium, magnesium and sodium as well as anionic components comprising carbonate, sulphate and nitrate. Part of the nitrate oxidizes 5 sulfite to sulfate.
10 15 20 25 30 « 3510 15 20 25 30 «35
Claims (5)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US9763987A | 1987-09-16 | 1987-09-16 | |
| US9763987 | 1987-09-16 |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| DK513988D0 DK513988D0 (en) | 1988-09-15 |
| DK513988A DK513988A (en) | 1989-06-28 |
| DK170605B1 true DK170605B1 (en) | 1995-11-13 |
Family
ID=22264412
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| DK513988A DK170605B1 (en) | 1987-09-16 | 1988-09-15 | Process for cleaning off exhaust gas |
Country Status (28)
| Country | Link |
|---|---|
| JP (1) | JPH01148330A (en) |
| KR (1) | KR890004760A (en) |
| CN (1) | CN1013642B (en) |
| AT (1) | AT395543B (en) |
| AU (1) | AU611478B2 (en) |
| BE (1) | BE1001118A5 (en) |
| BG (1) | BG49822A3 (en) |
| BR (1) | BR8804771A (en) |
| CA (1) | CA1311343C (en) |
| CH (1) | CH676437A5 (en) |
| DD (1) | DD273386A5 (en) |
| DE (1) | DE3830812A1 (en) |
| DK (1) | DK170605B1 (en) |
| ES (1) | ES2020810A6 (en) |
| FI (1) | FI884278A (en) |
| FR (1) | FR2620351B1 (en) |
| GB (1) | GB2210035B (en) |
| GR (1) | GR1000575B (en) |
| HU (1) | HU206642B (en) |
| IT (1) | IT1223827B (en) |
| NL (1) | NL8802265A (en) |
| NO (1) | NO884101L (en) |
| NZ (1) | NZ225964A (en) |
| PL (1) | PL274651A1 (en) |
| RO (1) | RO103174B1 (en) |
| SE (1) | SE8803286L (en) |
| YU (1) | YU175288A (en) |
| ZA (1) | ZA886879B (en) |
Families Citing this family (32)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04190831A (en) * | 1990-11-22 | 1992-07-09 | Hitachi Ltd | Recycling system for carbon dioxide as renewable resource |
| IL103918A (en) * | 1992-11-29 | 1996-10-16 | Hamit Energy As | Method for reducing atmospheric pollution caused by SO2 |
| DE4441628C2 (en) * | 1994-11-23 | 1998-06-18 | Binker Materialschutz Gmbh | Process for gassing a room |
| DE4441796A1 (en) * | 1994-11-24 | 1996-05-30 | Binker Materialschutz Gmbh | Method for drawing off toxic gas and neutralising it |
| JP2004261658A (en) * | 2003-02-26 | 2004-09-24 | Tokyo Electric Power Co Inc:The | Method for absorbing/fixing carbon dioxide in combustion exhaust gas |
| CN1309457C (en) * | 2003-12-30 | 2007-04-11 | 北京有色金属研究总院 | Method for treating waste gas of heating furnace of tester for testing gas in metal, and improved apparatus therefor |
| CN101553430A (en) * | 2006-08-29 | 2009-10-07 | 耶德研究和发展有限公司 | Methods and apparatuses for decreasing the CO2 concentration of a fluid |
| MX2009013821A (en) | 2007-06-28 | 2010-02-03 | Calera Corp | Desalination methods and systems that include carbonate compound precipitation. |
| US7753618B2 (en) | 2007-06-28 | 2010-07-13 | Calera Corporation | Rocks and aggregate, and methods of making and using the same |
| US20100239467A1 (en) | 2008-06-17 | 2010-09-23 | Brent Constantz | Methods and systems for utilizing waste sources of metal oxides |
| GB2460910B8 (en) | 2007-12-28 | 2010-07-14 | Calera Corp | Methods of sequestering CO2. |
| WO2010009273A1 (en) | 2008-07-16 | 2010-01-21 | Calera Corporation | Co2 utilization in electrochemical systems |
| WO2010008896A1 (en) | 2008-07-16 | 2010-01-21 | Calera Corporation | Low-energy 4-cell electrochemical system with carbon dioxide gas |
| US7993500B2 (en) | 2008-07-16 | 2011-08-09 | Calera Corporation | Gas diffusion anode and CO2 cathode electrolyte system |
| AU2009287462B2 (en) | 2008-09-30 | 2011-10-06 | Arelac, Inc. | CO2-sequestering formed building materials |
| US8869477B2 (en) | 2008-09-30 | 2014-10-28 | Calera Corporation | Formed building materials |
| US7939336B2 (en) | 2008-09-30 | 2011-05-10 | Calera Corporation | Compositions and methods using substances containing carbon |
| US7815880B2 (en) | 2008-09-30 | 2010-10-19 | Calera Corporation | Reduced-carbon footprint concrete compositions |
| US9133581B2 (en) | 2008-10-31 | 2015-09-15 | Calera Corporation | Non-cementitious compositions comprising vaterite and methods thereof |
| WO2010093716A1 (en) | 2009-02-10 | 2010-08-19 | Calera Corporation | Low-voltage alkaline production using hydrogen and electrocatlytic electrodes |
| JP2012519076A (en) * | 2009-03-02 | 2012-08-23 | カレラ コーポレイション | Gas flow complex contaminant control system and method |
| AU2010201373A1 (en) | 2009-03-10 | 2010-09-30 | Calera Corporation | System and methods for processing CO2 |
| US7993511B2 (en) | 2009-07-15 | 2011-08-09 | Calera Corporation | Electrochemical production of an alkaline solution using CO2 |
| US8864901B2 (en) | 2011-11-30 | 2014-10-21 | Boral Ip Holdings (Australia) Pty Limited | Calcium sulfoaluminate cement-containing inorganic polymer compositions and methods of making same |
| CN105903326A (en) * | 2016-06-14 | 2016-08-31 | 广东龙正节能环保科技有限公司 | Biomass ash desulfurization technology |
| CN106076106A (en) * | 2016-08-02 | 2016-11-09 | 山东大学 | A kind of semi-dry desulfurization and denitrification system and method based on biomass ash |
| CN111545031A (en) * | 2019-02-12 | 2020-08-18 | 源洁科技股份有限公司 | Fossil fuel pollutant control system |
| CN109746253A (en) * | 2019-03-18 | 2019-05-14 | 中冶南方都市环保工程技术股份有限公司 | The method and device of metallurgical slag collaboration processing incineration of refuse flyash |
| JP7356251B2 (en) * | 2019-04-01 | 2023-10-04 | 三菱重工業株式会社 | Apparatus and method related to gas purification treatment and/or combustion ash neutralization treatment |
| CN110064282A (en) * | 2019-04-10 | 2019-07-30 | 华电电力科学研究院有限公司 | A kind of high effective flue gas disappears whitening method and device |
| JP6683328B1 (en) * | 2019-04-16 | 2020-04-15 | 株式会社福岡建設合材 | Carbon dioxide concentration reducing method and carbon dioxide concentration reducing device |
| KR102306217B1 (en) * | 2021-06-09 | 2021-09-29 | 하이에어코리아 주식회사 | Apparatus and method for purifying exhaust gas of ship |
Family Cites Families (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU7386A1 (en) * | 1927-08-30 | 1928-12-31 | Н.Н. Емцов | Roller chain rail hinge |
| FR2205354A2 (en) * | 1972-11-03 | 1974-05-31 | Rhone Progil | Hydrogen chloride removal from gaseous incinerator emissions - by reacting with alkaline flue dust |
| JPS5210659B2 (en) * | 1973-04-09 | 1977-03-25 | ||
| US4002724A (en) * | 1973-10-11 | 1977-01-11 | Mckie R Thomas | Sulfur dioxide collection |
| DE2642326A1 (en) * | 1976-09-21 | 1978-03-23 | Saarbergwerke Ag | Removal of sulphur di:oxide from flue gases - by water scrubbing with neutralisation using alkaline fly ash |
| US4164547A (en) * | 1977-05-06 | 1979-08-14 | American Air Filter Company, Inc. | Process for removing sulfur dioxide in a wet scrubber |
| SU738645A1 (en) * | 1977-06-01 | 1980-06-05 | Московский Ордена Ленина И Трудового Красного Знамени Химико-Технологический Институт Им.Д.И. Менделеева | Method of purifying off-gases from acid components |
| DE2802018A1 (en) * | 1978-01-18 | 1979-07-19 | Fink Gerdinand | Refuse incinerator flue gas scrubber - with horizontal revolving drum and combustion residue pulp for washing |
| US4228139A (en) * | 1979-03-06 | 1980-10-14 | Peabody Process System, Inc. | Flue gas scrubbing process using fly ash alkali |
| DE3137359A1 (en) * | 1981-09-19 | 1983-04-14 | Ekkehard Prof. Dr.-Ing. 4300 Essen Weber | Process for treating waste waters from flue gas desulphurisation plants |
| DD213358A1 (en) * | 1983-02-07 | 1984-09-12 | Petrolchemisches Kombinat | PROCESS FOR ABSORPTION OF SULFUR DIOXIDE FROM EXHAUST GASES |
| DE3325140A1 (en) * | 1983-07-12 | 1985-01-31 | KABE Ingenierbüro GmbH, 2000 Hamburg | Process for the purification of dust- and aerosol-containing gases and/or vapours and unit for carrying out the process |
| DD247587A3 (en) * | 1983-11-03 | 1987-07-15 | Zittau Ing Hochschule | BINDING OF POLLUTANTS FROM EXHAUST GASOLATED COMBUSTION PLANTS BY MEANS OF ASH |
| DE3538231A1 (en) * | 1985-10-24 | 1987-04-30 | Mannesmann Ag | Process for reprocessing waste solutions |
| FR2590805B1 (en) * | 1985-12-02 | 1990-02-09 | Propiorga | PROCESS AND PLANT FOR THE NEUTRALIZATION OF ACID FUMES, ESPECIALLY FROM THE COMBUSTION OF RESIDUES |
-
1988
- 1988-08-29 NZ NZ225964A patent/NZ225964A/en unknown
- 1988-09-04 RO RO135160A patent/RO103174B1/en unknown
- 1988-09-09 DE DE3830812A patent/DE3830812A1/en not_active Ceased
- 1988-09-13 PL PL27465188A patent/PL274651A1/en unknown
- 1988-09-13 JP JP63227647A patent/JPH01148330A/en active Pending
- 1988-09-14 DD DD88319781A patent/DD273386A5/en not_active IP Right Cessation
- 1988-09-14 NL NL8802265A patent/NL8802265A/en not_active Application Discontinuation
- 1988-09-14 KR KR1019880011833A patent/KR890004760A/en not_active Application Discontinuation
- 1988-09-15 AT AT0226888A patent/AT395543B/en not_active IP Right Cessation
- 1988-09-15 BR BR8804771A patent/BR8804771A/en not_active Application Discontinuation
- 1988-09-15 NO NO88884101A patent/NO884101L/en unknown
- 1988-09-15 ES ES8802825A patent/ES2020810A6/en not_active Expired - Fee Related
- 1988-09-15 IT IT67822/88A patent/IT1223827B/en active
- 1988-09-15 CA CA000577455A patent/CA1311343C/en not_active Expired - Fee Related
- 1988-09-15 DK DK513988A patent/DK170605B1/en not_active IP Right Cessation
- 1988-09-15 AU AU22302/88A patent/AU611478B2/en not_active Ceased
- 1988-09-15 ZA ZA886879A patent/ZA886879B/en unknown
- 1988-09-15 CH CH3440/88A patent/CH676437A5/de not_active IP Right Cessation
- 1988-09-16 FI FI884278A patent/FI884278A/en not_active Application Discontinuation
- 1988-09-16 GR GR880100612A patent/GR1000575B/en unknown
- 1988-09-16 FR FR888812145A patent/FR2620351B1/en not_active Expired - Lifetime
- 1988-09-16 BG BG85445A patent/BG49822A3/en unknown
- 1988-09-16 HU HU884890A patent/HU206642B/en not_active IP Right Cessation
- 1988-09-16 GB GB8821734A patent/GB2210035B/en not_active Expired - Fee Related
- 1988-09-16 YU YU01752/88A patent/YU175288A/en unknown
- 1988-09-16 BE BE8801061A patent/BE1001118A5/en not_active IP Right Cessation
- 1988-09-16 CN CN88107168A patent/CN1013642B/en not_active Expired
- 1988-09-16 SE SE8803286A patent/SE8803286L/en not_active Application Discontinuation
Also Published As
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| DK170605B1 (en) | Process for cleaning off exhaust gas | |
| US5100633A (en) | Method for scrubbing pollutants from an exhaust gas stream | |
| US4915914A (en) | System for simultaneously scrubbing cement kiln exhaust gas and producing useful by-products therefrom | |
| KR930012036B1 (en) | Waste gas cleaning method and apparatus | |
| CA2070853C (en) | Method and apparatus for minimizing environmental release of toxic compounds in the incineration of wastes | |
| JP7356251B2 (en) | Apparatus and method related to gas purification treatment and/or combustion ash neutralization treatment | |
| JP2652669B2 (en) | Purification method of waste gas containing hydrochloric acid and sulfurous acid gas | |
| TWI795750B (en) | Apparatus and method for combustion exhaust gas purification | |
| US3961021A (en) | Method for removing sulfur dioxide from combustion exhaust gas | |
| WO1994018119A1 (en) | Method for scrubbing pollutants from an exhaust gas stream | |
| US3637347A (en) | Air pollution control system with chemical recovery | |
| EP0662859B1 (en) | Method and apparatus for cleaning a gas | |
| WO1994016992A1 (en) | Combined power environmental cycle (cpec) | |
| USRE33031E (en) | Method for simultaneously scrubbing cement kiln exhaust gas and producing useful by-products therefrom | |
| US4530292A (en) | Treatment of acidic organic and alkaline inorganic wastes | |
| CA1302049C (en) | Method and system for simultaneously scrubbing cement kiln exhaustgas and producing useful by-products therefrom | |
| CN214719281U (en) | Resource disposal system for incineration slag and fly ash | |
| RU86951U1 (en) | TECHNOLOGICAL LINE FOR INTEGRATED WASTE TREATMENT OF TITANIUM-MAGNESIUM PRODUCTION | |
| JP3354734B2 (en) | Method and apparatus for circulating fluidized bed combustion | |
| JP3519555B2 (en) | Exhaust gas treatment method for heavy oil fuel fired boiler | |
| EP0621854A1 (en) | Method and apparatus for desulfurization of a gas | |
| SE463076B (en) | PROCEDURES FOR SMOKE GAS TREATMENT | |
| CZ154890A3 (en) | Process of treating concentrated solution of sodium sulfite, sulfate and thiosulfate | |
| CS269260B1 (en) | Method of hydrogen fluoride and hydrogen chloride removal from sour gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| B1 | Patent granted (law 1993) | ||
| PBP | Patent lapsed |