EP0293424A1

EP0293424A1 - PROCESS FOR REDUCING FLUE GAS NO x? EMISSION FROM FIRING INSTALLATIONS

Info

Publication number: EP0293424A1
Application number: EP19870907928
Authority: EP
Inventors: Georg Gebhard; Heinz HÖLTER; Ernst-Peter Dr. Uerpmann
Original assignee: Holter Heinz Dipl-Ing
Current assignee: Holter Heinz Dipl-Ing
Priority date: 1986-12-18
Filing date: 1987-12-04
Publication date: 1988-12-07
Also published as: WO1988004571A1; DE3729482A1

Abstract

Procédé de réduction de l'émission de NOx accompagnant les gaz brûlés, par mise en contact du jet de gaz avec des microparticules tensio-actives.Process for reducing the NOx emission accompanying the burnt gases, by bringing the gas jet into contact with surface-active microparticles.

Description

Process for reducing NO emissions of flue gases from combustion plants

Description

The invention relates to a method for reducing NO emissions of flue gases from combustion plants.

Λ

NO is a collective term for the different oxides of nitrogen, especially nitrogen monoxide

(NO) and nitrogen dioxide (NO), which are formed during the combustion of fossil fuels in combustion plants and pollute the flue gas by up to 0.1 percent by volume. In conventional combustion plants, the proportion of nitrogen monoxide is about 95 percent by volume, that of

Nitrogen dioxide is generally less than 5 percent by volume and is largely formed on the way from the combustion system to the chimney outlet.

The harmful effects of nitrogen oxides are known, and laws and regulations have been in force in the Federal Republic of Germany for more than a decade a reduction in emissions of nitrogen oxides is required. NO limit values were determined, which are also calculated as NO «in mg / m 3 R ^X.

According to the last targets set by the Environment Ministers' Conference for NO emissions from large combustion plants

NO limit values for plants with a capacity over 300 MW betw een ^x 100 and 200 mg _N0? / m3 flue gas.

Various measures for reducing the NO emissions are known, which are basically divided into primary measures which restrict the formation of NO compounds and secondary measures which reduce the content of NO gases in the flue gases.

The lowering of the oxygen concentration and / or the combustion temperature in the flame area are known, for example, as primary firing measures.

Through different air / fuel exposure, the use of low-NO burners and / or water / Daπrp -. the NOx limit values can be reduced injectively.

However, the success is highly plant-specific and depends on the fuel properties. The secondary measures include methods of reducing the NOx Verbindunq ³ e 'n into nitrogen (N "), the gas remains in the flue gas, or oxidation of the nitrogen monoxide to Stickstoff¬ dioxide, which is dissolved in aqueous phase and in the form of nitrate by-product arises.

In the so-called "SNCR process" ammonia (NH „) is burned in excess at temperatures between 850 ° and 1000 ° C, the reduction of nitrogen monoxide being faster than the combustion of ammonia. Part of the excess ammonia reacts with oxygen to form nitrogen Substance and water, the rest of it enters the atmosphere in downstream systems and possibly via the chimney.

At lower temperatures, the reactions mentioned only take place with the support of catalysts, for example activated carbon, zeolite or titanium dioxide catalysts, the nitrogen oxides being reduced to nitrogen using ammonia. In the case of a reduction process using activated coke as a catalyst, it is a prerequisite that S0 "in the flue gas is largely removed before the addition of ammonia, since otherwise ammonium sulfate forms and occupies the activated coke.

A disadvantage of all processes is that sometimes complex and expensive special systems have to be set up. A disadvantage is above all that simultaneous separation of nitrogen and sulfur oxides is not possible. Rather, the systems are usually connected in series.

The combination of the above-mentioned "SNCR technology" (selective πoπcatalytic reduction) with a subsequent flue gas desulfurization was described from a lecture on the occasion of a special event organized by the Association of Large Power Plant Operators on June 11 and 12, 1986. The flue gas is then taken over from a melting chamber furnace and passed into a catalyzer at 350 ° to 400 ° C. After the "denitrification", ceramic preheaters, electric filters, limestone smoke gas sulfurization systems and again a ceramic preheater are flowed through. The system is complicated and requires a large amount of space. Problems with the above-mentioned methods continue to exist due to the contamination of downstream power plant components such as heating surfaces, air preheaters, blowers and / or flue gas desulfurization systems.

It has also been proposed to connect a denitrification system downstream of a flue gas desulfurization system. However, this usually requires the flue gases to be reheated.

At the aforementioned conference of the Association of Large Power Plant Operators (op. Cit.), Options for simultaneous desulfurization and NO reduction using the "SHL process (Saarberg-Hölter-Lurgi process)" were also reported. Although an S0 _? - and NO cleaning of flue gases takes place, the known method has so far remained in the experimental stage because of the need for complex regeneration of the washing solution.

In this respect, the invention is based on the object of specifying a possibility for reducing NO emissions from flue gases from combustion plants, which results in the lowest possible NO emissions, the aim being preferably at the same time to use a simultaneous SO _p - Combine cleaning of the flue gases. Finally, it is also an object of the invention to optimize the process to the extent that it can preferably be used in conventional plants, in particular conventional flue gas desulfurization.

The invention is based on the knowledge that a drastic reduction in the NO content in the flue gas stream can be achieved by a sufficient number of free Surfaces of very fine particles are made available within the washing suspension of the flue gas desulfurization system, namely those very fine particles which are suitable for absorbing and / or adsorbing nitrogen oxides on their surface or for reacting with them.

The invention is therefore in complete contradiction to the prior art. According to the prior art, the proportion of very fine particles (suspended matter) in the washing suspension must be kept deliberately low (preferably zero). The prior art assumes that this is the only way that the formation of the calcium sulfate hydrate products is not adversely affected or that no dewatering problems occur. The state of the art has hitherto always assumed that only the desulfurization of the flue gases is carried out in the flue gas desulfurization system, namely by absorption of the sulfur dioxide from the flue gases with the aid of appropriate absorption agents (for example limestone), this process being as little as possible to be disturbed.

Surprisingly, it has now been shown that a conscious increase in the proportion of very fine particles with a particle size below 10 μ can easily be accepted without disturbing the flue gas desulfurization and in this way at the same time a medium for the absorption and / or adsorption of or reaction is provided with the nitrogen oxides of the flue gas.

The method according to the invention is characterized by the features of claim 1. Advantageous further developments result from the features of the claims and the other application documents. Various materials have proven to be particularly advantageous. Primarily ^'are here clays and clay minerals may be mentioned, in particular those from the smectite, vermiculite and / or mica group relate huπgsweise other silicates, and hydrates thereof, for example, volcanic rocks or the like.

Although the mechanism of action has not yet been fully elucidated, it can be assumed that these substances contribute to a catalytic reaction of the nitrogen oxides with the sulfur oxides.

The corresponding very fine particles can be added as such to a conventional washing suspension, for example a limestone washing suspension, or can be prepared to a suspension with water.

Likewise, however, it is also possible to use as fine particles those from the sewage sludge of the water treatment of a power plant, whereby this sewage sludge often also at least partially contains the mineral components mentioned above. By using the sewage sludge, a disposal product is usefully used for further use. Experiments have shown that the quenching of the corresponding coarse ash in the process water may also result in a further activation of the free surfaces of the mineral components or may promote new mineral formation.

The waste materials from limestone processing, which may also contain fumed or silicate components, have also proven to be suitable.

It has also surprisingly been found that unburned constituents, for example from wet ash, coarse ash and / or fly ash, enable a power plant firing to have the desired effect. Wet ash is understood to mean an exhausted kettle ash which has unburned heavy particles. In contrast, one speaks of coarse ash in unleached ashes.

The coarse ash essentially consists of quartz, silicates such as clays or mica, calcium oxide and unburned coal.

In an advantageous embodiment of the method according to the invention, in order to optimize the NO bond, it is proposed to recycle the flue gas scrubber, that is to say to increase the proportion of very fine particles within the scrubbing suspension or, in other words, to thicken the scrubbing suspension. In this way, the fine particle content can be increased and adjusted so that the ^" best possible NO binding is achieved. In this case, only an excess material flow is then withdrawn from the circulating water of the desulfurization system.

Experiments have shown that the circulating water should preferably be run with a proportion of the fine particles above 50 ml / l, this proportion being able to be increased up to 1000 ml / l, with higher solids contents preferred in the sense of a NO Λ reduction in the flue gas stream become.

In other words, this means that the proportion of very fine particles, based on the total washing medium, can preferably be at least 5% by weight or, according to an advantageous embodiment of the invention, up to 100% by weight.

According to a further advantageous proposal of the invention, the degree of separation of the nitrogen oxides can be increased. of trace elements, such as iron, manganese, chromium, copper, nickel, cobalt, zinc, lead, strontium and / or boron salts in the aqueous phase are improved, obviously they also influence the oxidation of nitrogen oxides in a catalytic manner.

The trace elements can be added separately to the washing suspension, but in some cases they can also be introduced via the impurities in the limestone used as an absorption medium for desulfurization.

The degree of separation of NO or N0 _? is otherwise improved if the temperature of the aqueous phase is set to above 45 ° C, preferably between 45 ° and 65 ° C.

In order to optimize the N0 / N0 _p deposition, the pH of the wash suspension should also preferably be between 4 and 7.

The problems of a fine particle fraction described in the prior art have already been referred to above. Nevertheless, it has not only proven to be possible, but in the sense of simultaneous desulfurization and separation of the nitrogen oxides, to use only the sewage sludge from the water treatment of a power plant, preferably the upstream power plant itself, as the absorbent in the desulfurization plant and then, if appropriate thicken the wash suspension in the manner described above.

In addition to the aforementioned influence of the various fine particles, the invention has also recognized that the degree of oxidation in the flue gas is important in relation to the reduction of NO emissions from flue gases from combustion plants has. The degree of oxidation is the volume ratio of nitrogen dioxide to the sum of nitrogen monoxide and nitrogen dioxide (multiplied by 100). Accordingly, in an advantageous embodiment, which can also be seen as an alternative, the invention proposes to set the degree of oxidation of the flue gas to a value between 5% and 50%. Measures for this are given below as examples.

The degree of oxidation can be adjusted by both primary and secondary measures.

From the point of view of a simultaneous separation of NO and SO _p compounds, it is particularly advantageous to carry them out directly in existing wet flue gas desulfurization plants.

For preferably directly increasing the NOp proportion, on the one hand, firing measures of a known type are suitable, such as the use of low-NO Λ burners in the combustion system or the reduction in the combustion temperature of the flue gases.

However, it is particularly advantageous to use nitrogen-containing compounds, in particular ammonia, to form N0 _? to burn. Instead of ammonia, urea, NH.0H, liquid manure or municipal sewage sludge can also be burned to form 0 _p , which has the advantage that problem or residual material is simultaneously removed in this way.

N0p then obviously reacts additionally to NO to form nitrous oxide (N _p 0 "), which is in the water (in the washing suspension) with the formation of nitrate (NO.) or nitrite (N0 _? ) is relatively easily soluble, the nitrite then reacting with HS0 "to form various NS compounds, from which nitrogen (N") and sulfate are then formed is, the latter reacting with the Ca ions of the wash suspension to calcium sulfite / calcium sulfate products.

The intermediate reactions have not yet been fully clarified. "

It is crucial that by adding N0 _? the reaction to the easily water-soluble nitrous oxide is promoted. In ammonia combustion, for example on noble metal catalysts (for example titanium dioxide catalysts), large amounts of nitrogen dioxide are formed, which then go into the flue gas.

In addition to the described setting of the degree of oxidation of the flue gases to values between 5% and 50% (the degree of oxidation of a conventional flue gas is between 1% and a maximum of 5%), the invention also proposes further manipulations of the wash suspension.

According to an advantageous embodiment of the invention, the washing suspension should contain hydrogen peroxide (H _p O _p )

_{* be} added. Eberiso can be added to ozone to oxidize the nitrogen oxides.

It has also proven to be suitable for the washing suspension of the flue gas desulfurization system to contain nitrates as alkali and / or alkaline earth nitrates, preferably calcium and / or sodium nitrates in solid and / or liquid form to admit. The increase in the NO "content in the laundry sump then leads to the advantages described above.

The separation of the nitrogen oxides is further improved by adding nitrogen-containing compounds, such as ammonium salts or urea, which are NH ₃ , NH ^ H, (NH ₄ ) ₂ S0 ₄ , NH..CL, (NH ₄ ) N0 ₃ , NH ₄ CL, (NH ₄ ) _p _CO ₃ and / or (NH ₂ ) ₂ CO in solid and / or dissolved form are added, the NO _p with these substances being known in a manner known per se, in particular within the preferred temperature range of the washing suspension converts to nitrogen. A smaller proportion of NH can also be introduced directly via the exhaust gas.

If, according to the invention, one speaks of a wet flue gas cleaning process, this term also includes spray absorption processes in an analogous application.

The idea of the invention can also be used quite generally in flue gas cleaning systems connected downstream of combustion systems.

The method according to the invention leads to a reduction of the NO emissions by up to 90 percent, depending on the type and amount of the catalysts used and / or adsorbent / adsorbent.

Claims

P a t e n t a n s r u c h e

A process for Miπderunq ^a NOx - emission of Ra uch - gases from Feuerungsanlageπ in a so-called Naß¬ wash with a content of fines with a grain size of 10 microns in the scrubbing suspension, the

Very fine particles are such materials that 'superficially absorb or adsorb the NOx compounds or react with them and react with the SO _{p of} the flue gas to form N _? and / or NS connections.

2. The method according to claim 1 with the proviso that as

Fine particles from the group of clays and clay minerals, in particular those from the smectite, vermiculite and / or mica group and / or other silicates and their hydrates, are used.

3. The method according to claim 1 or 2 with the proviso that as fine particles such from the sewage sludge water treatment of a power plant are used.

4. The method according to any one of claims 1 to 3 with the proviso that the waste materials from limestone processing are used as fine particles.

5. The method according to any one of claims 1 to 4 with the

Provided that unburned constituents from the wet ash, coarse ash and / or fly ash of a power plant fire are used as the fine particles.

6. The method according to any one of claims 1 to 5, wherein the solid stream in the wash suspension is thickened, for example in a circuit, to adjust a predetermined fine particle fraction, and in each case only one excess solid fraction is withdrawn with the circulating water to achieve a predetermined degree of denitrification.

7. The method according to any one of claims 1 to 6, wherein the Feinstteilchenanteil is adjusted to at least 5 wt .-% of the overall ^• samtwäschermediums.

8. The method according to any one of claims 1 to 7, wherein the fine particle content is set to at least 10, preferably at least 20 wt .-% of the total washing medium.

9. The method according to any one of claims 1 to 8 with the proviso that the washing suspension trace elements, in particular heavy metal salts, in particular iron, manganese chromium, copper, nickel, cobalt, zinc, lead, stron¬ tium - And / or boron salts are added in solid and / or dissolved form.

10. The method according to claim 9 with the proviso that as

Trace elements impurities of the limestone used as an absorbent for desulfurization are introduced.

11. The method according to any one of claims 1 to 10, wherein the washing suspension at a temperature above

45 ° C, preferably between 45 ° and 65 ° C.

12. The method according to any one of claims 1 to 11, wherein the pH of the wash suspension is adjusted between 4 and 7.

13. The method according to any one of claims 1 to 12 with the proviso that the solids content of the absorbent of the flue gas scrubbing is provided exclusively by the solids content of the sewage sludge of the water treatment of a power plant.

14. The method according to any one of claims 1 to 13, wherein

NO the degree of oxidation (2 100) of the flue gases

N0 + NQ, a value between 5% and 50% is set before the flue gas is introduced into the flue gas desulfurization system.