EP3734158A1 - Verfahren zur reduktion von stickoxiden und kohlenmonoxid in den ofenkammern von wasser- und dampfkesseln, insbesondere von rostkesseln, und system zur reduktion von stickoxiden und kohlenmonoxid in den ofenkammern von wasser- und dampfkesseln, insbesondere von rostkesseln - Google Patents

Verfahren zur reduktion von stickoxiden und kohlenmonoxid in den ofenkammern von wasser- und dampfkesseln, insbesondere von rostkesseln, und system zur reduktion von stickoxiden und kohlenmonoxid in den ofenkammern von wasser- und dampfkesseln, insbesondere von rostkesseln Download PDF

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Publication number
EP3734158A1
EP3734158A1 EP20020236.4A EP20020236A EP3734158A1 EP 3734158 A1 EP3734158 A1 EP 3734158A1 EP 20020236 A EP20020236 A EP 20020236A EP 3734158 A1 EP3734158 A1 EP 3734158A1
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EP
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Prior art keywords
furnace chamber
process gas
reagent
lances
injection
Prior art date
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Granted
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EP20020236.4A
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English (en)
French (fr)
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EP3734158B1 (de
EP3734158C0 (de
Inventor
Dariusz Szewczyk
Andrzej Pasiewicz
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Ics Industrial Complete Solutions SA
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Ics Industrial Combustion Systems SA
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Publication of EP3734158C0 publication Critical patent/EP3734158C0/de
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J7/00—Arrangement of devices for supplying chemicals to fire
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C9/00—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2202/00—Fluegas recirculation

Definitions

  • the object of the invention is a method for the reduction of nitrogen oxides and carbon monoxide in the furnace chambers of water and steam boilers, especially grate boilers and a system for the reduction of nitrogen oxides and carbon monoxide in the furnace chambers of water and steam boilers, especially grate boilers, used to reduce the formation of nitrogen oxides and carbon monoxide and/or their reduction in the furnace chambers of heating boilers and power boilers, especially grate boilers, and a system for the application of this method.
  • the method described in the patent application P.423576 assumes that the process gas, or process gas and reagent, are injected into the furnace chamber in the opposite direction to the main natural direction of the flue gas flow through the chamber, preferably from top to bottom, i.e. in the case of injection from the top, side or front wall of the firebox, in the direction of temperature rise in the furnace chamber, and in the case of process gas injection through lances from the back wall of the firebox, as an additional reinforcement of the swirl, the process gas is supplied horizontally, with a jet deviation of +/-45°, in a plane parallel to the longitudinal symmetry plane of the furnace chamber.
  • the process gas injection points are located on the front, top, side or rear wall of the furnace chamber, while the reagent and process gas injection points are located on the front, side or top wall of the furnace chamber, while the process gas injection points are located at a distance of up to 0.5 depth of the furnace chamber from the pipe axis of the front screen while when process gas is injected from the rear wall of the furnace chamber, the injection points are located at a distance of up to 0.2 depth of the furnace chamber from the pipe axis of the rear screen of the chamber.
  • the above described method of feeding process gas or process gas and reagent causes a flue gas stream of high NO X concentration at the rear wall of the furnace chamber, on a significant part of the boiler width, and the described method of feeding process gas and reagent through lances mounted on the side walls of the boiler furnace chamber makes it possible for the reagent to enter this stream and reduce NO X compounds in this area.
  • the technical problem to be solved is how to eliminate the abovementioned drawbacks and limitations, while guaranteeing further reduction of NO X emissions, reduction of CO emissions, minimising or completely eliminating the reagent in flue gases and fly ashes, increasing the efficiency of the system and lowering operating costs.
  • the essence of the invention which is a method for the reduction of nitrogen oxides and carbon monoxide in the furnace chambers of water and steam boilers, especially grate boilers consists in that process gas, being air, flue gas or combustion air mixture, in its full range, i.e.
  • process gas is supplied to the furnace chamber at a speed of 30 to 180 m/s, preferably 135 m/s, in the amount of up to 20% of stoichiometric air demand necessary to burn the fuel supplied to the boiler, preferably 15%, with up to 60% of the process gas being injected via lances built into the front screen of the furnace chamber, with 60% of the process gas being injected through lances installed on the rear screen of the furnace chamber, up to 25% of the process gas is injected through lances installed on the upper screen of the furnace chamber and up to 15% of the process gas is injected through lances installed on the side screens of the furnace chamber; moreover, the reagent is delivered to the furnace chamber at a rate of 30 to 180 m/s, preferably 135 m
  • temperature and the share of O 2 , CO or NO X in the flue gas such parameters being monitored by measuring devices mounted inside the furnace chamber in the form of temperature sensors and/or devices mounted outside the furnace chamber being the flue gas analyser, and the regulation is carried out by means of actuators individually for each injection point or group of injection points mounted on a given wall of the furnace chamber, on a given level or with a specific injection direction.
  • This method is realized in a system according to the invention, for the reduction of nitrogen oxides and carbon monoxide in furnace chambers of water boilers and steam boilers, especially grate boilers, containing a process gas feeder with a flow regulator, process gas lances, a device measuring the concentration of NOx, CO or NOx, CO and O 2 in flue gases and a controller, the essence of which consists in that the process gas feeder comprising an intake, which through an air duct on which the control and cut-off damper is mounted, is connected to the flue gas duct, through which the flue gas is taken from the section of the flue gas duct connecting the dedusting or dedusting and desulfurizing system with the chimney, and on this duct there is also a control and cut-off throttle, by means of which the ratio of air to flue gases in the process gas is regulated, then through the common duct the process gas is sucked in by the process gas fan and pumped from the process gas feeder to the process gas delivery duct, on the process gas duct
  • a liquid or gaseous reagent is injected centrally through at least one lance into the process gas collector.
  • the reagent is injected into the furnace chamber together with the process gas through nozzles installed inside the process gas injection lances, where the number of reagent nozzles is equal or lower than the number of process gas lances.
  • the reagent is injected into the furnace chamber by means of nozzles installed between the process gas injection lances at the level of the process gas lances, and the number of reagent lances is equal to or lower than the number of process gas lances.
  • the process gas is supplied to the lances directly from the fan and the reagent is supplied directly from the zonal control and cut-off components.
  • the dynamic effect of the process gas stream was used to intensify the mixing process in the furnace chamber by inducing strong internal flue gas recirculation inside the furnace chamber and a strong swirl whose direction is opposite to the main, natural flue gas flow direction and the swirl plane is parallel to the longitudinal symmetry plane of the furnace chamber.
  • the solution according to the method allows for precise control of the temperature in the furnace chamber in the area where nitrogen oxides are reduced and CO is burned, reducing the concentration of the reagent in the furnace chamber, which minimises the risk of corrosion of the equipment components; moreover, the invention according to one of the embodiments, increases the capacity of the system by placing the lances on several levels of the furnace chamber, especially in the case of a considerable variability of the boiler load and this is usually used in units with higher power output.
  • the invention according to the method also reduces reagent consumption in relation to known methods and thus allows to minimize the content of unreacted reagent in fly ashes and flue gases, which plays a very important role in terms of system operating costs, environmental protection and ash management.
  • the opposite direction of reagent injection in relation to the main, natural direction of flue gas flow and to the inside of the generated swirls, as well as the described points and directions of injection have a very important advantage in relation to the traditional directions and places of reagent injection cited in the state of the art investigation, because in the described method according to the invention, there is no such phenomenon (or if it occurs it is limited to a minimum) as entrainment of unreacted reagent particles, directly after it has been injected into the furnace chamber by the flue gases into the convection part of the boiler, i.e.
  • the reduction reaction takes place in the temperature range from 850°C to 1050°C and in the presence of nitrogen compounds; further on, the unreacted particles of the reagent enter the temperature area above 1050°C where they bind with oxygen and form NO X -type compounds, which then, together with the products of combustion, head up the furnace chamber in accordance with the main natural draught of the combustion chamber where they encounter the unreacted reagent and the temperature conditions required for the occurrence of the NOX reduction reaction; part of the still unreacted reagent and unreacted nitrogen compounds (NOX) are returned to an area convenient for the NOX reduction reaction, through strong swirls of recirculating flue gas produced by the process gas stream.
  • NOX nitrogen compounds
  • This natural and spontaneous course of the process contributes to the efficiency of the reduction process and to a large extent protects the system against the ingress of unreacted reagent into the ash, dust or flue gas treatment and discharge systems;
  • another advantage of the method according to the invention is that the process gas is injected into the furnace chamber in the opposite direction to the natural direction of the flue gas movement in the furnace chamber and at a high rate turns back towards the grate i.e. into the high temperature area, particles of unburned coal, which in the hitherto known solutions are entrained from the layer of coal moving on the grate by the blast air supplied from the grate and, as coal, together with fly ashes enter the dust extraction systems significantly reducing their efficiency.
  • the presented method according to the invention significantly reduces the content of the carbon element in fly ash, which directly contributes to the increase in the efficiency of the system and also reduces the amount of fly ash carried by the flue gases leaving the boiler and entering the dedusting systems, which extends the service life of the devices and in newly built units enables the use of smaller first-stage dedusting systems reducing the equipment cost. This effect is particularly noticeable when burning poorer quality coal containing a lot of coal fines.
  • the presented method of feeding the process gas or process gas and reagent produces a strong, main, reverse internal recirculation swirl and, depending on the boiler capacity, one to two additional swirls, one called the upper swirl, which is formed in the area bounded by the front screen, the upper and the stream of process gas injected from the lances mounted on the rear screen of the furnace chamber, this swirl being particularly noticeable at medium and high boiler loads, and a second one, called the down swirl, which is formed in the area bounded by the rear screen, the grate deck and the flue gas stream moving from the front zones of the grate towards the rear screen and further on towards the festoon, this swirl being particularly noticeable at low boiler loads;
  • the main swirl and the upper swirl generated at medium and high boiler loads suck in flue gases from the main flue gas stream, from the area just before the furnace chamber is connected to the convection line, and thus create optimal conditions for nitrogen oxide reduction and carbon monoxide afterburning, with minimal oxygen content in flue gas and minimum amount of reagent entering the chimney
  • Figure 1 shows the block diagram of the system for the realization of the method where: 4 - is the furnace chamber, 5 - is the front process gas/reagent collector, 6 - is the front process gas injection lance, 7 - is the front reagent injection lance/nozzle, 8 - is the convection part of the boiler, 9 - is the rear process gas collector, 10 - is the rear reagent injection lance, 11 - is the upper process gas/reagent collector, 12 - is the upper process gas injection lance, 13 - is the upper reagent injection lance, 15 - is the side process gas/reagent collector, 16 - is the side process gas injection lance, 17 - is the side reagent injection lance, 18 - is the process gas intake, 19 - is the control and shut-off component of the process gas feeder - air system, 20 - is the control and shut-off component of the process gas feeder - flue gas system, 21 - is the process gas fan, 22 - is the measuring system installed on the process gas collector, 23
  • Figure 2 shows in a schematic and illustrative manner the place of installation of process gas and reagent injection lances, as well as the flow lines and swirl directions which occur during combustion in the furnace chamber of the equipment, preferably a grate boiler, where: 1 - is the sub-grate box of air, 2 - is the layer of fuel moving on the grate, 3 - is the grate, 4 - is the furnace chamber, 5 - is the front process gas/reagent collector, 6 - is the front process gas injection lance, 7 - is the front reagent injection lance/nozzle, 8 - is the convection part of the boiler, 9 - is the rear process gas collector, 10 - is the rear reagent injection lance, 11 - is the top process gas/reagent collector, 12 - is the top process gas injection lance, 13 - is the top injection lance of the reagent, 14 - is the temperature sensor, 15 - is the side collector of the process gas/reagent, 16 - is the side injection la
  • FIG. 2 The example embodiment according to the method will be illustrated by Fig. 2 in which A is the primary air pumped by the blast air fan to the control valves and then to the sub-grate boxes 1, whose task is to dose the oxidant in a controlled way to fuel 2 moving on the grate 3.
  • A is the primary air pumped by the blast air fan to the control valves and then to the sub-grate boxes 1, whose task is to dose the oxidant in a controlled way to fuel 2 moving on the grate 3.
  • fuel is burned and the amount of oxidant supplied in the form of primary air A ranges from 0.7 to 1.3 of the amount of stoichiometric air needed for full and complete combustion of fuel 2, preferably less than 1.0, moving on grate 3 as defined by the standards for this type of equipment.
  • process gas (PG) or process gas and reagent (PG+R) are injected through collector 5 mounted outside the chamber, up to 60% of the process gas supplied to the system, through a series of lances 6 and 7 made and installed in such a way that the direction of injection of process gas (PG) or process gas with reagent (PG+R) is opposite to the main direction of flow through the furnace chamber 4 with a jet deviation of +/-15° in the plane parallel to the longitudinal symmetry plane of the furnace chamber, whereby part of the process gas (PG) or process gas with reagent (PG+R) accounting for up to 20% of the total amount of the process gas or process gas and reagent fed through lance
  • process gas (PG) accounting for up to 60% of the process gas supplied to the system through collector 9 built in the convection part of boiler 8 and through lances 10 mounted on the rear wall of the furnace chamber 4, at the level of the lower edge of the boiler festoon is injected in the direction of grate 3 at an angle of 45°, and this angle is measured between the centre line of the jet and the back wall of the furnace chamber and another portion of process gas (PG) or process gas and reagent (PG+R) accounting for up to 25% of the process gas supplied to the system, via collector 11 mounted outside the boiler furnace chamber and through lances 12 and 13 mounted on the upper wall of the boiler furnace chamber 4 is injected in the opposite direction to the main direction of the FG flow through furnace chamber 4, whereby injection from each of lances 12 and/or 13 is made from at least one point, with a jet deviation of up to +/- 60° in the plane parallel to the longitudinal symmetry plane of the furnace chamber; the remaining process gas (PG) or process gas and
  • the injection rate of process gas (PG) or reagent (R) is from 30 to 180 m/s, preferably 135 m/s, and the process gas stream accounts for up to 20% of the air stream necessary for full and complete combustion of the fuel as defined by the standards for this type of equipment; due to high speed, significant mass of the process gas stream and the way it is fed into the furnace chamber, a strong internal recirculation of iFGR flue gas inside furnace chamber 4 and a strong main swirl (MS) are produced, and depending on the boiler capacity, one or two additional swirls, one called upper swirl (US) and the other called down swirl (DS); the swirls rotate in a plane parallel to the longitudinal symmetry plane of the furnace chamber.
  • a strong internal recirculation of iFGR flue gas inside furnace chamber 4 and a strong main swirl (MS) are produced, and depending on the boiler capacity, one or two additional swirls, one called upper swirl (US) and the other called down swirl (DS); the swirls rotate in a plane parallel to the longitudinal symmetry plane of
  • Lance 6 and 7 are shaped similarly to letter "L" and are introduced through deflections made in the front wall of furnace chamber 4. Thanks to the way in which lance 6 and 7 are fixed, it possible to change their position in the plane parallel to the longitudinal plane of symmetry of the boiler by +/- 15°.
  • the back lances 10 are mounted directly in the boiler festoon or are introduced through the deflections made in the back wall of furnace chamber 4.
  • the top lances 12 and 13 are mounted on the ceiling of furnace chamber 4 and are introduced through deflections made in this wall and each of the lances has at least one injection point.
  • such a method of feeding process gas PG and reagent R is conducive to creating favourable conditions for conducting the process of nitrogen oxide reduction with very high efficiency due to the fact that the reagent after injection into furnace chamber 4 mixes with the injected process gas and combustion products moving in the direction of the temperature rise, i.e.
  • the reduction reaction takes place in a temperature range from 850°C to 1050°C and in the presence of nitrogen oxides; the excess unreacted reagent R is transported to an area of increasingly higher temperature where the unreacted reagent reacts with oxygen and forms nitrogen oxides, which then, together with the products of combustion, head up the furnace chamber in a direction consistent with the main natural draught in the furnace chamber, where they encounter an unreacted reagent and suitable temperature conditions for the occurrence of the reduction reaction; part of the still unreacted reagent and unreduced nitrogen compounds (NO X ) just before leaving the furnace chamber is returned to the area with suitable conditions for the reduction reaction by a strong stream of recirculating exhaust gas produced by the process gas stream.
  • NO X still unreacted reagent and unreduced nitrogen compounds
  • the feeding of process gas and reagent in a manner according to the invention creates a strong main reverse swirl parallel to the longitudinal plane of symmetry of the furnace chamber and, depending on the boiler output, additionally an upward or downward swirl, which rotate in the same plane as the main swirl but in opposite directions; as a result, the system is, in a broad spectrum of operation, a self-regulating system, thus protecting itself against the ingress of unreacted reagent into the exhaust gases and ashes; moreover, the system according to the invention is hardly sensitive to fluctuations in the amount of nitrogen oxides produced in the process of burning fuel on the grate.
  • the process gas is injected into the furnace chamber in the opposite direction to the natural direction of the flue gas movement in the furnace chamber and at high rate, it returns towards the grate, i.e. into the high-temperature area, particles of unburned coal, which in the hitherto known solutions, are entrained from the layer of coal moving on the grate by the blast air supplied from the grate and, as coal, enter together with fly ashes into the dust extraction systems, significantly reducing the overall equipment efficiency.
  • the presented method significantly reduces carbon content in fly ashes, which directly contributes to the increase in boiler efficiency, as well as reduction in the amount of fly ashes captured by flue gases leaving the boiler and the content of unreacted reagent in such ashes entering the dedusting systems, resulting in the extension of the service life of these units due to the reduction of erosion and corrosion of the equipment and in newly built units allows for the use of smaller first-stage dedusting systems, reducing the related costs.
  • the invention may be used in all applications where emphasis is placed on high quality of the combustion process, low emissions, especially of nitrogen oxides and carbon monoxide, investment savings, energy savings, and reagent savings, i.e. operating costs.
  • the method presented in the description is intended for use in heating boilers and power boilers, especially grate-type boilers.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Regulation And Control Of Combustion (AREA)
EP20020236.4A 2019-03-21 2020-05-19 Verfahren zur Reduzierung von Stickoxiden und Kohlenmonoxid in Feuerkammern von Wasser- und Dampfkesseln, insbesondere Rostkesseln. Active EP3734158B1 (de)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PL429343A PL429343A1 (pl) 2019-03-21 2019-03-21 Sposób redukcji tlenków azotu oraz tlenku węgla w komorach paleniskowych kotłów wodnych i kotłów parowych, szczególnie kotłów rusztowych oraz układ do redukcji tlenków azotu i tlenku węgla w komorach paleniskowych kotłów wodnych i kotłów parowych, szczególnie kotłów rusztowych

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EP3734158A1 true EP3734158A1 (de) 2020-11-04
EP3734158B1 EP3734158B1 (de) 2024-07-31
EP3734158C0 EP3734158C0 (de) 2024-07-31

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Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1995015463A1 (en) 1993-12-03 1995-06-08 Hagstroem Ulf A method and a feeding apparatus for controlling mixing conditions in a combustion or gasification plant
US5809910A (en) * 1992-05-18 1998-09-22 Svendssen; Allan Reduction and admixture method in incineration unit for reduction of contaminants
WO2004085922A2 (en) 2003-03-19 2004-10-07 Mobotec Usa Inc. Mixing process for combustion furnaces
US20060118013A1 (en) 2003-09-09 2006-06-08 Marx Peter D Method and apparatus for adding reducing agent to secondary overfire air stream
PL196745B1 (pl) 2000-01-14 2008-01-31 Ecomb Ab Urządzenie doprowadzające płyn do komory spalania urządzenia wytwarzającego ciepło
CN101545630A (zh) * 2009-04-30 2009-09-30 宁波怡诺能源科技有限公司 一种控制烟气含氧量燃煤锅炉
WO2013009566A2 (en) 2011-07-08 2013-01-17 Baker Hughes Incorporated Method of curing thermoplastic polymer for shape memory material
US20130244190A1 (en) * 2010-09-29 2013-09-19 Fortum Corporation Oxygen combustion system and method for operating same
US20130291772A1 (en) * 2010-09-30 2013-11-07 Babcock-Hitachi Kabushiki Kaisha Combustion system and method for operating same
US20160003473A1 (en) 2014-07-04 2016-01-07 Alstom Technology Ltd BOILER AND A METHOD FOR NOx EMISSION CONTROL FROM A BOILER
CN106051749A (zh) * 2016-05-27 2016-10-26 青岛金田热电有限公司 一种基于循环流化床锅炉的低氮燃烧工艺
US20170261206A1 (en) * 2014-09-12 2017-09-14 Mitsubishi Heavy Industries Environmental & Chemical Engineering Co., Ltd. Stoker-type incinerator

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5809910A (en) * 1992-05-18 1998-09-22 Svendssen; Allan Reduction and admixture method in incineration unit for reduction of contaminants
WO1995015463A1 (en) 1993-12-03 1995-06-08 Hagstroem Ulf A method and a feeding apparatus for controlling mixing conditions in a combustion or gasification plant
PL196745B1 (pl) 2000-01-14 2008-01-31 Ecomb Ab Urządzenie doprowadzające płyn do komory spalania urządzenia wytwarzającego ciepło
WO2004085922A2 (en) 2003-03-19 2004-10-07 Mobotec Usa Inc. Mixing process for combustion furnaces
US20060118013A1 (en) 2003-09-09 2006-06-08 Marx Peter D Method and apparatus for adding reducing agent to secondary overfire air stream
CN101545630A (zh) * 2009-04-30 2009-09-30 宁波怡诺能源科技有限公司 一种控制烟气含氧量燃煤锅炉
US20130244190A1 (en) * 2010-09-29 2013-09-19 Fortum Corporation Oxygen combustion system and method for operating same
US20130291772A1 (en) * 2010-09-30 2013-11-07 Babcock-Hitachi Kabushiki Kaisha Combustion system and method for operating same
WO2013009566A2 (en) 2011-07-08 2013-01-17 Baker Hughes Incorporated Method of curing thermoplastic polymer for shape memory material
US20160003473A1 (en) 2014-07-04 2016-01-07 Alstom Technology Ltd BOILER AND A METHOD FOR NOx EMISSION CONTROL FROM A BOILER
US20170261206A1 (en) * 2014-09-12 2017-09-14 Mitsubishi Heavy Industries Environmental & Chemical Engineering Co., Ltd. Stoker-type incinerator
CN106051749A (zh) * 2016-05-27 2016-10-26 青岛金田热电有限公司 一种基于循环流化床锅炉的低氮燃烧工艺

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EP3734158C0 (de) 2024-07-31
PL429343A1 (pl) 2020-10-05

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