Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
  • F23J15/00—Arrangements of devices for treating smoke or fumes
  • F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
  • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
  • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
  • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
  • F23G5/12—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating using gaseous or liquid fuel
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
  • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
  • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
  • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
  • F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
  • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
  • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
  • F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
  • F23G7/066—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
  • F23J15/00—Arrangements of devices for treating smoke or fumes
  • F23J15/006—Layout of treatment plant
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
  • F23L15/00—Heating of air supplied for combustion
  • F23L15/04—Arrangements of recuperators
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
  • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2209/00—Specific waste
  • F23G2209/14—Gaseous waste or fumes
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
  • F23K2900/00—Special features of, or arrangements for fuel supplies
  • F23K2900/01041—Heating by using exhaust gas heat

Definitions

• Low calorific value waste fuels and in particular low calorific value waste gases, are generated by various industrial processes, such as processes of the chemical, metallurgical and cement industries, of the energy sector (gasification process of biological fractions), agri-food sector (e.g. various types of fermentation processes), etc.
• One type of a low calorific value gas is waste gas with a high nitrogen content.
• Polish patent application P.438329 discloses a method and device for the combustion of low calorific value gas, in which fuel gas burned in a separate burner is used for the combustion of low calorific value waste gas by means of a flare burner.
• the fuel gas is mainly propane and/or butane converted from the form of a liquid gas referred to as LPG to the gaseous phase by supplying thermal energy via a set of suitable exchangers.
• Polish patent PL2533B1 discloses a system and method for low-emission combustion of waste gases, especially of a low calorific value, in combustion chambers of industrial energy conversion devices, in which a mixture of waste gas, a full-value fuel and air is subjected to combustion.
• a mixture of waste gas, a full-value fuel and air is subjected to combustion.
• an air chamber is fed with a continuous stream of air, which is then fed into a first combustion segment, where the air velocity is increased, and the air is mixed with the full-value fuel.
• This mixture is then ignited by a pilot burner which initiates and sustains the flame and, in turn, the resulting hot flue gases heat the consecutive segments of the combustion system.
• waste gas is fed into the first combustion segment via a nozzle.
• waste gas is introduced sequentially thereinto.
• first and second flue gas heaters for the oxidant are connected to an oxidant duct for heating the oxidant before its introduction into the combustion chamber
• first and second flue gas heaters for the low calorific value fuel are connected to a low calorific value fuel duct for heating the low calorific value fuel before its introduction into the combustion chamber.
• the system comprises a flue gas heater for water, and a turbine system with an electric generator driven by steam from the flue gas heater for water.
• the system comprises a first steam heater for the oxidant, fluidly connected to the second flue gas heater for the oxidant and located in a steam duct.
• a first steam heater for the oxidant fluidly connected to the second flue gas heater for the oxidant and located in a steam duct.
• the system comprises a steam heater for the low calorific value fuel, fluidly connected to the second flue gas heater for the low calorific value fuel and located in the steam duct.
• a steam heater for the low calorific value fuel fluidly connected to the second flue gas heater for the low calorific value fuel and located in the steam duct.
• the system comprises a steam heater for water, fluidly connected to the flue gas heater for water and located in the steam duct downstream of the steam heater for the low calorific value fuel.
• the heat of the steam is used to preheat the water before its introduction into the flue gas heater for water.
• the system comprises a flue gas heater for the process medium, located in the flue gas duct.
• the system contains at least one steam heater for the process medium.
• the system can be adapted to the technological needs of the customer.
• the object of the invention is also a low calorific value fuel combustion method in a low calorific value fuel combustion system, comprising the steps of: heating the semi-adiabatic combustion chamber by means of the starting fuel from ambient temperature up to a temperature of 750°C; a fuel with a heating value of less than 2.5 MJ/Nm 3 , and in particular with a heating value of less than 2.1 MJ/Nm 3 , being supplied as the low calorific value fuel.
• the low calorific value fuel is introduced into the second flue gas heater for the low calorific value fuel; the low calorific value fuel is preheated in the second flue gas heater for the low calorific value fuel; subsequently, in the first flue gas heater for the low calorific value fuel, the preheated low calorific value fuel is heated up to a target temperature of up to 800°C; the oxidant is introduced into the second flue gas heater for the oxidant; the oxidant is preheated in the second flue gas heater for the oxidant; subsequently, in the first flue gas heater for the oxidant, the preheated oxidant is heated up to a target temperature of up to 800°C, following which the heated oxidant is introduced into the combustion chamber, and the heated low calorific value fuel is introduced into the combustion chamber.
• the low calorific value fuel is preheated in the first steam heater for the low calorific value fuel.
• the oxidant is preheated in the first steam heater for the oxidant.
• the oxidant is heated in a second steam heater, located in the steam duct downstream of the first steam heater for the oxidant.
• a fuel with a heating value of less than 2.1 MJ/Nm 3 is supplied as the low calorific value fuel.
• Fig. 1 presents schematically a flue gas system for a low calorific value waste fuel combustion system in a first embodiment.
• Fig. 6 presents a diagram of a particular embodiment of the system according to the invention.
• Fig. 7 presents an embodiment of a flue gas duct with flue gas heaters.
• Fig. 8 presents an embodiment of the system with a semi-adiabatic chamber connected to the flue gas duct.
• the low calorific value fuel combustion system comprises a semi-adiabatic combustion chamber 10 connected to a flue gas 7 duct 27 and having a burner 26 for a starting fuel 6, a nozzle 81 for introducing low calorific value fuel 8, and a nozzle 91 for introducing an oxidant 9.
• the system further comprises the following placed in the flue gas 7 duct 27: a first flue gas heater 41 for the oxidant 9, a first flue gas heater 31 for the low calorific value fuel 8, a second flue gas heater 42 for the oxidant 9, fluidly connected to the first flue gas heater 41 for the oxidant 9, a second flue gas heater 32 for the low calorific value fuel 8, fluidly connected to the first flue gas heater 31 for the low calorific value fuel 8.
• the starting fuel 6, e.g. a high calorific value gas, is only used to pre-heat the combustion chamber 10. The rest of the process takes place without the use of the starting fuel 6.
• the oxidant 9 can be air, a mixture of air with an addition of flue gases, a mixture of air with an addition of oxygen, or a mixture of air with an addition of oxygen and flue gases.
• the low calorific value fuel 8 is a fuel with a heating value of less than 2.5 MJ/Nm 3 , which can, for example, be a low calorific value gas, and in particular a waste gas with a high inert gas content of at least 84%.
• the flue gas heaters 41, 31, 42, 32 have the form of heat exchangers that absorb heat from the flue gas 7 and transfer it to the medium-the oxidant 9-or to the low calorific value fuel 8-flowing therethrough.
• the heaters heat exchangers
• the heaters are continuously operating shell or tube heat exchangers, mounted alternately (oxidant 9, low calorific value fuel 8) and in a multi-stage arrangement (at least two-stage heating of the oxidant 9, at least two-stage heating of the low calorific value fuel 8).
• a series of alternately mounted flue gas heaters 41, 31, 42, 32 (that is, at least two flue gas heat exchangers 31, 32 for heating the low calorific value fuel 8 and at least two flue gas heat exchangers 41, 42 for heating the oxidant 9) located in the flue gas 7 duct 27 allow for multi-stage heating of the combustion process substrates before their introduction into the combustion chamber 10.
• the flue gas heaters 41, 42 for the oxidant 9 are connected via the oxidant 9 duct 29 to a source of the oxidant 9
• the flue gas heaters 31,32 for the low calorific value fuel 8 are connected via the low calorific value fuel 8 duct 28 to a source of low calorific value fuel.
• the system allows for two-stage heating of the oxidant (e.g. air) to a target temperature of 600°C and for two-stage heating of the low calorific value fuel 8 (e.g. waste gas with a high nitrogen content) to a temperature of 450°C.
• the oxidant e.g. air
• the low calorific value fuel 8 e.g. waste gas with a high nitrogen content
• the flue gas heaters 31, 32, 41, 42 are mounted alternately, so that the first flue gas heater 41 for the oxidant 9 is located first in the flue gas 7 duct 27 and is followed sequentially by: the first flue gas heater 31 for the low calorific value fuel 8, the second flue gas heater 42 for the oxidant 9, fluidly connected to the first flue gas heater 41 for the oxidant 9, and the second flue gas heater 32 for the low calorific value fuel 8, fluidly connected to the first flue gas heater 31 for the low calorific value fuel 8.
• the flue gas heaters 31, 32, 41, 42 are mounted alternately, so that the first flue gas heater 41 for the oxidant 9 is located first in the flue gas 7 duct 27 and is followed sequentially by: the first flue gas heater 31 for the low calorific value fuel 8, the second flue gas heater 42 for the oxidant 9, fluidly connected to the first flue gas heater 41 for the oxidant 9, and the second flue gas heater 32 for the low calorific value fuel 8, fluidly connected to
• the order in which the exchangers are mounted may change, i.e. so that the first flue gas heater 31 for the low calorific value fuel 8 is positioned first in the flue gas 7 duct 27, and it is followed sequentially by the first flue gas heater 41 for the oxidant 9, the second flue gas heater 32 for the low calorific value fuel 8, and the second flue gas heater 42 for the oxidant 9.
• air at a temperature of 20°C is preheated to a temperature of 250°C in the second flue gas heater 42 for the oxidant 9, and subsequently it is heated in the first flue gas heater 41 for the oxidant 9 to a target temperature of 600°C.
• low calorific value gas 8 is preheated to a temperature of 200°C in the second flue gas heater 32 for the low calorific value fuel 8, and subsequently it is heated in the first flue gas heater 31 for the low calorific value fuel 8 to a target temperature of 450°C.
• the thermal energy from the combustion of the low calorific value waste fuel 8 is transferred into substrates supplied to the combustion process, resulting in an increase in the adiabatic combustion temperature, stabilising the combustion process.
• the process is characterised by very high efficiency and does not require supplying additional energy in the form of high calorific value fuel gases to conduct and sustain the combustion process.
• a semi-adiabatic combustion chamber 10 allows for performing zonal volumetric combustion using zonal (gradual) injection of the fuel (e.g. low calorific value gas) and the oxidant into the combustion chamber 10.
• the fuel e.g. low calorific value gas
• the low calorific value fuel combustion system may comprise a first flue gas heater 51 for water 5 and a turbine system 11 (preferably with a twin-screw turbine) with an electric generator 4 driven by steam 3 (wet steam-containing a mixture of steam and water) generated in the first flue gas heater 51 for water 5.
• Fig. 3 presents schematically a third embodiment of the system, with a steam generation system and an electricity generation system.
• the first flue gas heater 51 for water 5 has the form of an evaporator, which generates the steam 3 used further down in the system.
• the first flue gas heater 51 for water may be located downstream of the last flue gas heater 32 for the low calorific value fuel 8.
• the system may comprise a first steam heater 43 for the oxidant 9, fluidly connected to the second flue gas heater 42 for the oxidant 9 and located in a steam 3 duct 13.
• the oxidant (e.g. air) 9 is first preheated in the first steam heater 43 for the oxidant 9, and then passes sequentially to the second and first flue gas heaters 42, 41 for the oxidant 9.
• the oxidant e.g. air
• system may comprise a steam heater 33 for the low calorific value fuel 8, fluidly connected to the second flue gas heater 32 for the low calorific value fuel 8 and located in the steam 3 duct 13.
• the system may comprise a steam heater 52 for water 5, fluidly connected to the first flue gas heater 51 for water 5 and located in the steam 3 duct 13 downstream of the steam heater 33 for the low calorific value fuel 8. The heat of the steam 3 is then used to preheat the water 5 before its introduction into the first flue gas heater 51 for water 5.
• the system may comprise a flue gas heater 53 for the steam 3, fluidly connected to the first flue gas heater 51 for water 5.
• a flue gas heater 53 for the steam 3 is located in the flue gas 7 duct 27 upstream of the second flue gas heater 42 for the oxidant 9.
• system may comprise a second flue gas heater 54 for water 5, for preheating the water 5 before its introduction into the first flue gas heater 51 for water 5.
• the system comprises a condensate cooler 15 connected to the steam heater 52 for water 5 and a feedwater 5 tank 16 connected to the condensate cooler 15 and connected to the steam heater 52 for water.
• the system may comprise a water 5 preparation station 20, fluidly connected to the water tank 16. Before the water 5 is introduced into the tank 16, it is purified of undesirable compounds to the required system parameters, which takes place in the water preparation station 20.
• Fig. 2 presents schematically a second embodiment of the low calorific value waste fuel combustion system with flue gas heaters for process media.
• the system comprises at least two flue gas heaters 24, 25 for the process medium 2, located in the flue gas 7 duct 27, downstream of the flue gas heaters for the oxidant 9 and low calorific value fuel 8.
• An example of a process medium 2 can be process oil, process gas, hot utility water, water in a central heating system, etc.
• the system may also comprise at least one steam heater 21, 22, 23 for the process medium 2 ( Figs. 5 , 6 ).
• the system may include systems for introducing other additional low calorific value fuels 1 into the combustion process, varying in composition and varying in the calorific value, as well as varying in flow per a time unit, which can be introduced into the combustion system during the operation of the primary waste fuel disposal system, providing an additional amount of energy.
• Fig. 4 presents schematically the system of Fig. 3 with a system for the combustion of an additional low calorific value fuel.
• the invention also relates to a method for the combustion of low calorific value fuel in the low calorific value fuel combustion system shown above.
• the low calorific value fuel combustion method comprises steps in which a semi-adiabatic combustion chamber 10 is heated with the starting fuel 6 from ambient temperature up to a temperature of 750°C, wherein a fuel with a heating value of less than 2.5 MJ/Nm 3 is supplied as the low calorific value fuel.
• the low calorific value fuel 8 is introduced into the second flue gas heater 32 for the low calorific value fuel 8
• the low calorific value fuel 8 is preheated in the second flue gas heater 32 for the low calorific value fuel 8.
• the low calorific value fuel 8 is heated up to a target temperature of up to 800°C.
• the oxidant 9 is introduced into the second flue gas heater 42 for the oxidant 9, and the oxidant 9 is preheated in the second flue gas heater 42 for the oxidant 9.
• the oxidant 9 is then heated in the first flue gas heater 41 for the oxidant 9 up to a target temperature of up to 800°C, following which the heated oxidant 9 is introduced into the combustion chamber 10, and the heated low calorific value fuel 8 is introduced into the combustion chamber 10.
• the combustion process for the low calorific value fuel is carried out at a temperature of 750°C to 850°C.
• the low calorific value fuel 8 is preheated in the steam heater 33 for the low calorific value fuel 8.
• the efficiency of the system is increased. As a result, it is possible to achieve a higher temperature of the low calorific value fuel 8.
• the oxidant 9 is preheated in the first steam heater 43 for the oxidant 9.
• the oxidant 9 is preheated in the first steam heater 43 for the oxidant 9.
• the low calorific value fuel 8 is heated in a third flue gas heater 34 for the low calorific value fuel 8, which is located in the flue gas 7 duct 27 downstream of the second flue gas heater 32 for the low calorific value fuel 8.
• a third flue gas heater 34 for the low calorific value fuel 8 which is located in the flue gas 7 duct 27 downstream of the second flue gas heater 32 for the low calorific value fuel 8.
• the use of a larger number of heaters allows for maximising the use of energy from steam and flue gases, and for increasing the efficiency of the system.
• the exchangers By locating the exchangers in the most convenient location for heating the process media in terms of temperature, the system can be adapted to the technological needs of the customer.
• the oxidant 9 is heated in a second steam heater 44, located in the steam 3 duct 13 downstream of the first steam heater 43 for the oxidant 9.
• a second steam heater 44 located in the steam 3 duct 13 downstream of the first steam heater 43 for the oxidant 9.
• the low calorific value fuel combustion system comprises two flue gas heaters 41, 42 for the oxidant 9, three flue gas heaters 31, 32, 34 for the low calorific value fuel 8 arranged alternately with the flue gas heaters 41, 42 for the oxidant 9 in the flue gas 7 duct 27, one steam heater 33 for the low calorific value fuel 8, and two steam heaters 43, 44 for the oxidant 9 arranged alternately in the steam 3 duct 13 downstream of the turbine system 11 with the electric generator.
• Air at a temperature of 20°C was introduced into the second steam heater 44 for the oxidant, and the air was heated up to a temperature of 85°C. Then the air was heated in the first steam heater 43 for the oxidant from a temperature of 85°C to a temperature of 130°C. Subsequently, the air was heated from a temperature of 130°C to a temperature of 235°C in the second flue gas heater 42 for the oxidant, followed by heating the air from a temperature of 235°C to a target temperature of 600°C in the first flue gas heater 41 for the oxidant 9.
• low calorific value gas 8 at a temperature of 20°C was introduced into the steam heater 33 for the low calorific value fuel 8, and the low calorific value gas 8 was heated up to a temperature of 90°C. Subsequently, in the third flue gas heater 34 for the low calorific value fuel 8, the low calorific value gas was heated up from a temperature of 90°C to a temperature of 140°C.
• the low calorific value gas 8 was heated up from a temperature of 140°C to a temperature of 215°C, followed by heating the low calorific value gas 8 from a temperature of 215°C to a target temperature of 450°C in the first flue gas heater 31 for the low calorific value fuel 8.
• the air and low calorific value gas thus heated were introduced into a semi-adiabatic combustion chamber 10. Wherein the semi-adiabatic combustion chamber 10 was heated in advance to a temperature of 750°C using starting fuel 6. The combustion process for the low calorific value fuel was then carried out at a temperature of 750°C to 850°C.
• the presented system and method allow for the utilisation of low calorific value and ultra-low calorific value fuel, e.g. waste gas with a significant content of inert non-combustible components, including, e.g. nitrogen, through its efficient low-emission volumetric combustion, with no need to consume additional high-calorific value afterburning fuel (e.g. natural gas, LPG, etc.) to sustain the combustion process.
• low calorific value and ultra-low calorific value fuel e.g. waste gas with a significant content of inert non-combustible components, including, e.g. nitrogen
• the presented system and method do not require the use of additional complex catalytic systems necessary to lower the activation energy in order to sustain a stable combustion process at a lower temperature, the use of which has the following main disadvantages: a complex thermal energy recovery system, sensitivity of the catalyst bed to contaminants and substances carried by waste fuel, the need for periodic regeneration or replacement of the catalyst bed, the need to consume high-calorific value fuel in the process, especially for ultra-low calorific value gases, and a lower temperature of the process.
• the presented system and method do not require the use of complex regenerative heating systems for heating the substrates in order to conduct a stable combustion process, the use of which has the following main disadvantages: a complex system of regenerative substrate heaters, sensitivity of regenerators to contaminants and substances carried by waste fuel, the need for periodic replacement of regenerators, the risk of underfiring of the combustible parts due to the regenerative/switching nature of the substrate heating system, and high investment costs.
• the presented system and method ensure high heating of the substrates fed into the combustion chamber, which results in an increase in the adiabatic combustion temperature, and consequently contributes to stabilisation of the combustion process.
• high-calorific value fuel to sustain the combustion process.
• the presented system and method allow for the combustion of waste fuels with a heating value below 2.5 MJ/Nm 3 with no need to use additional high calorific value fuel to sustain the combustion process, and with no need to use complex regenerative heating systems or complex catalytic systems to lower the activation energy in order to sustain a stable combustion process at a lower temperature.
• the multi-stage and alternating heating system for the substrates of the combustion process also allows for the installation of additional exchangers for heating other process media required for any on-site technological process. It is also possible to use systems generating electricity based on low-temperature steam circuits.
• the compact, component-based design of the system allows for its application at the place where the waste fuel (of a low calorific value and ultra-low calorific value) is present (generated).

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