WO2014007679A1 - Procédé et régulation de chauffage d'air et dispositif de sa mise en oeuvre - Google Patents

Procédé et régulation de chauffage d'air et dispositif de sa mise en oeuvre Download PDF

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Publication number
WO2014007679A1
WO2014007679A1 PCT/RU2013/000557 RU2013000557W WO2014007679A1 WO 2014007679 A1 WO2014007679 A1 WO 2014007679A1 RU 2013000557 W RU2013000557 W RU 2013000557W WO 2014007679 A1 WO2014007679 A1 WO 2014007679A1
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WO
WIPO (PCT)
Prior art keywords
air
fuel
oxidation products
oxidation
heating
Prior art date
Application number
PCT/RU2013/000557
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English (en)
Russian (ru)
Inventor
Андрей Владиславович КУРОЧКИН
Original Assignee
Kurochkin Andrei Vladislavovich
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Kurochkin Andrei Vladislavovich filed Critical Kurochkin Andrei Vladislavovich
Publication of WO2014007679A1 publication Critical patent/WO2014007679A1/fr

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Classifications

    • 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 
    • F23C13/00—Apparatus in which combustion takes place in the presence of catalytic material
    • 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
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • 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
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N5/00—Systems for controlling combustion
    • F23N5/003—Systems for controlling combustion using detectors sensitive to combustion gas properties
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • the invention relates to methods, devices and methods for regulating direct heating of air by mixing with products of oxidation (combustion) of hydrocarbon fuels and can find application in the oil and gas, chemical, metallurgical and other industries, as well as in municipal and agricultural sectors.
  • the air is heated by mixing carbon- and / or water containing hydrogen-containing gaseous or liquid fuel with a part of the air taken with a coefficient of excess from 1 to 5 to stoichiometric and preheated to the temperature of the catalytic oxidation process by heat exchange with at least part of the oxidation products, obtaining a gaseous fuel mixture, its catalytic oxidation to carbon dioxide and water, and mixing the oxidation products with the remaining part of the air, while the maximum temperature of the oxidation products p dderzhivayut at 10- 50 ° C below the temperature stability of the catalyst, but not higher than 900 ° C.
  • a device for heating air including a heat exchange section for heating air with oxidation products, a heated air and fuel mixer, a starting heater, a catalytic cassette and a mixer of oxidation products with air, as well as a method for controlling the air heating process by adjusting the air heating temperature by changing the air flow rate, controlling the temperature pre-heating part of the air by changing the flow rate of part of the oxidation products sent to the heat exchange section Nia maximum temperature oxidation products by changes in the coefficient of excess air in the fuel mixture.
  • the use of the invention allows the use of not only hydrocarbon gases as fuel, but also low-calorific gas mixtures containing an increased amount of non-combustible gases (carbon dioxide, nitrogen, water vapor, etc.), as well as liquid distillate fuel, including gas condensate, unstable gasoline and other types of light hydrocarbon fuels, and at the same time receive heated air in a wide temperature range, minimally contaminated with carbon monoxide and nitrogen oxides.
  • the invention relates to methods, devices for heating air and methods for regulating direct heating of air by mixing with products of oxidation (combustion) of hydrocarbon fuels and may find application in the oil and gas, chemical, metallurgical and other industries, as well as in public utilities and agriculture.
  • the circle of consumers of heated air is extremely diverse.
  • the most common way to produce heated air is to heat it by the heat of flame burning various types of hydrocarbon fuels with the transfer of heat to the heated air, either through a heat exchange surface, or by direct mixing with combustion products.
  • unresolved problems are minimization of emissions of nitrogen oxides and carbon monoxide generated in the flame at temperatures above 1000 ° C, as well as the high fire and explosion hazard of the process.
  • the devices "Thermocat-1" and “Thermocat-2” operate on liquefied gas - propanbutane mixture, and the device “Thermocat-3" - on natural gas. These air heaters use full oxidation catalysts of the type IR-12-30.
  • a gas mixing catalytic air heater [Z.R. Ismagilov, M.A. Kerzhentsev, “Ecologically clean burning of fuels and catalytic purification of flue gases of TPPs from nitrogen oxides: state and prospects” Journal of the All-Union Chemical Society named after D.I. Mendeleev, 1991, v. 35, issue 1, p. 43-54].
  • the air heater is a two-stage natural gas combustion plant. At the first stage, flaring of natural gas is carried out. Then the flue gases, additionally diluted with air, are fed into the second chamber, where a catalytic cassette, assembled from hexagonal blocks of a honeycomb catalyst catalyst, is installed.
  • the temperature of the flue gases in front of the catalytic cartridge 427-827 ° C is sufficient for the partial reduction of nitrogen oxides with excess carbon monoxide, as well as the oxidation of products of incomplete combustion of fuel and carbon monoxide with atmospheric oxygen.
  • the mixture of oxidation products is additionally diluted with air and used to heat the room.
  • the flame burning of fuel in the first stage in a torch burner leads to the formation of nitrogen oxides, which cannot be completely restored in the second catalytic stage, as well as soot particles.
  • the presence of unreacted methane in the products of flame combustion leads to the formation of a “hot spot” in the frontal part of the catalytic cassette, which causes thermal destruction of the catalyst.
  • IPC F24H3 / 00 which are two-stage devices burning gaseous fuels with flame burning fuel in the first stage and catalytic or flame burning (oxidation) of products of incomplete combustion with additional fuel in the second stage, followed by mixing the combustion products with the required amount of cold air.
  • the fuel mixture is obtained in an air and fuel mixer.
  • the catalyst used is a reinforced porous material containing active components: rhodium, nickel, platinum, palladium, iron, cobalt, rhenium, ruthenium, or a mixture thereof.
  • a catalytic oxidation reactor was also used, in which the products of incomplete oxidation (combustion) of the first stage fuel are oxidized (burned) to carbon dioxide and water vapor with additional air.
  • the products of complete oxidation of the fuel practically free of CO and nitrogen oxides, are mixed with the required amount of air, obtaining heated air of the required temperature.
  • the temperature control of the heated air is carried out by a coordinated change in the flow rate of gaseous fuel and the air flow rate for mixing with the products of oxidation (combustion) of the fuel.
  • the known method and device does not allow the use of liquid fuel, and conducting air heating in two stages complicates the process.
  • the start of the air heater requires pre-heating of the catalyst to a temperature of more than 600 ° C, which requires increased energy consumption and leads to a large inertia of the startup device.
  • the objective of the invention is to expand the range of fuels used, simplifying the design of the device, reducing the inertia of starting the device into operation while maintaining the completeness of fuel combustion and minimizing the pollution of heated air WITH and nitrogen oxides.
  • the specified technical result is achieved by the fact that in the method of operation of the air heater, which consists in mixing fuel with part of the heated air to obtain a gaseous fuel mixture, catalytically oxidizing the fuel mixture to carbon dioxide and water, and mixing the oxidation products with the remaining part of the heated air, according to the invention, the fuel mixture obtained by mixing gaseous or liquid distillate fuel and part of the heated air taken with a coefficient of excess from 1 to 5 to stoichiometric and oxidation catalyst preheated to a lower temperature limit due to heat exchange with at least part of the oxidation products, while the maximum temperature of the oxidation products is maintained at 10-50 ° C below the temperature of thermal stability of the catalyst, but not higher than 950 ° C.
  • the method is carried out using a device for heating air, including an air and fuel mixer, a starting heater, a catalytic cassette and a mixer of oxidation products with air, in which according to the invention, it is additionally contains a heat exchange section for preheating air with oxidation products, as well as valves installed on the air supply line to the oxidation product mixer with air, on the fuel supply line to the air and fuel mixer, and also on the bypass line at the outlet of the oxidation products from the catalytic section.
  • a device for heating air including an air and fuel mixer, a starting heater, a catalytic cassette and a mixer of oxidation products with air
  • it is additionally contains a heat exchange section for preheating air with oxidation products, as well as valves installed on the air supply line to the oxidation product mixer with air, on the fuel supply line to the air and fuel mixer, and also on the bypass line at the outlet of the oxidation products from the catalytic section.
  • a catalytic cartridge section
  • a reactor with a radial input of raw materials containing a fixed bed of granular catalyst or a reactor with a block-cell catalyst.
  • Air heating is carried out using a control method that provides for a coordinated change in fuel consumption and air consumption for mixing with fuel oxidation (combustion) products, in which, according to the invention, air heating temperature is controlled by changing the fuel consumption by a valve mounted on the fuel supply line to the air mixer and fuel, the temperature control of the preheating of part of the air is carried out by changing the flow rate of part of the oxidation products directed to heat an exchange section, a valve mounted on the bypass line at the outlet of the oxidation products from the catalytic section, while regulating the maximum temperature of the oxidation products is carried out by changing the excess air ratio of the fuel mixture by a valve mounted on the air supply line with air mixer oxidation products.
  • the mixture of fuel and part of the air preheated to the lower temperature limit of the oxidation catalyst, due to heat exchange with at least part of the oxidation products provides the possibility of using not only natural gas, but also low-calorific gas mixtures containing an increased amount of non-combustible gases (carbon dioxide) gas nitrogen water vapor, etc.), as well as liquid distillate fuel, which forms a gaseous fuel mixture due to evaporation in excess of hot air.
  • liquid fuels used such as gas condensate, unstable gasoline and other types of light hydrocarbon fuels, which are not applicable for flame combustion due to high fire and explosion hazard.
  • Oxidation of the fuel mixture containing air with an excess coefficient from 1 to 5 to stoichiometric allows maintaining the maximum temperature in the catalyst layer in the optimal temperature range (450-900 ° C depending on the chemical composition of the fuel), on the one hand, not exceeding the temperature of the thermostability of the catalyst, and on the other hand, ensuring the complete oxidation of fuel to carbon dioxide and water without the formation of nitrogen oxides and CO.
  • the heat exchange section for preheating the air with oxidation products provides heating of the air to the lower temperature limit of the oxidation catalyst, which contributes to the efficient operation of the entire catalyst volume and the low-inertia start of the device.
  • a heat exchange section a heat exchanger with temperature-unloaded heat exchange elements (self-compensating), for example, a twisted type or a spiral-radial type, is used.
  • the catalyst provides the minimum hydraulic resistance of the air heater and the minimum energy consumption for driving a pressure fan or smoke exhaust.
  • Regulation of the temperature of heating the air by changing the fuel consumption provides the ability to set the temperature of heating the air in the temperature range from +10 to + 650 ° C to ambient temperature.
  • the temperature control of the preheating of part of the air by changing the flow rate of part of the oxidation products sent to the heat exchange section makes it possible to maintain the required temperature of the fuel mixture and stable operation of the oxidation catalyst when the thermal performance of the device changes.
  • the proposed method of heating air is as follows.
  • the air heating circuit is shown in the drawing.
  • the air (I) entering the air heater is divided into two parts, one of which (II) is fed to the heat exchange section 1, where it is heated to the lower temperature limit of the oxidation catalyst (280-530 ° C depending on the chemical composition of the fuel and the type of catalyst )
  • the other part of the air (III) through the valve 2 is fed into the mixer 3 for mixing with the oxidation products (IV).
  • the heated air in the mixer 4 is mixed with the gaseous or liquid fuel (V) supplied through the valve 5.
  • the gaseous fuel mixture (VI) obtained as a result of evaporation of liquid fuel and mixing of its vapors with air (or mixing of gaseous fuel with air), sent to the catalytic section 6, where there is a complete oxidation of the fuel to carbon dioxide and water.
  • Oxidation products with a temperature not exceeding 900 ° C are divided into two parts, one of which (VII) is sent to the inlet of the heat exchange section 1 for heating the air, and the other (VIII) is supplied through the valve 7 to the output of the heat exchange section 1 in line oxidized products cooled by air.
  • the resulting mixture of oxidation products is sent to a mixer 3, where it is mixed with a stream of air (III) to produce heated air (IX).
  • the air in front of the mixer 4 is heated using the starting heater 9 to the lower temperature limit of the oxidation catalyst, for example, by means of electric heating.
  • the low heat capacity of the air combined with the possibility of supplying at start-up a relatively small amount of air and fuel, as well as the need for heating only for a temperature of 280-530 ° C, provides low power consumption and low inertia of the device during start-up.
  • Carbon and / or hydrogen-containing fuels are used as fuel, including hydrocarbon gases, low-calorie gas mixtures containing an increased amount of non-combustible gases (carbon dioxide, nitrogen, water vapor, etc.), liquid distillate fuel, including kerosene, diesel fuel, distillate marine fuel, various types of light hydrocarbon fuels, such as gas condensate, unstable gasoline.
  • a catalytic cartridge can be used a reactor with a radial input of raw materials containing a fixed bed of granular catalyst, or a reactor with a block-cell catalyst with low hydraulic resistance and high specific surface area of the catalyst.
  • a method of heating air has not been found, including mixing gaseous or liquid fuels with a portion of air taken 1-5 times excess, and pre-heated to the lower temperature limit of the operation of the oxidation catalyst due to heat exchange with oxidation products, catalytic oxidation - the resulting fuel mixture to carbon dioxide and water, and the mixture of oxidation products with the rest of the air.
  • Example 1 Stable gas condensate is mixed with a 5-fold excess of air heated to 350 ° C and sent to the catalytic section with a block honeycomb magnesium-chromium catalyst, oxidation products with a temperature of 680 ° C are partially sent to a heat exchange section made in in the form of a heat exchanger with twisted tubular elements, where it is cooled to 380 ° C, mixed with an additional amount of ambient air and receive air with a temperature of 50 ° C, used to heat the room.
  • the content of CO in heated air is less than 1 rh, nitrogen oxides are absent.
  • Example 2 Associated petroleum gas is mixed with a 4-fold excess of air heated to 390 ° C, and sent to the catalytic section with a radial inlet with alumina-chromium granular catalyst, oxidation products with a temperature of 790 ° C are partially sent to the heat-exchange section of the spiral-radial type where it is cooled to 340 ° C, mixed with an additional amount of ambient air and receive air with a temperature of 300 ° C, used for heating process equipment.
  • the CO content in heated air is about 1 ppm; nitrogen oxides are absent.
  • the content of CO in heated air is 1, 5 rh, nitrogen oxides are absent.
  • the proposed method and device can be used in the oil and gas, chemical, metallurgical and other industries, as well as in public utilities and agriculture.
  • the invention is reproducible and when used, its purpose is realized.
  • the claimed invention meets the patentability criterion of "industrial applicability".

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)

Abstract

L'invention concerne le génie énergétique et peut s'utiliser pour produire de l'air chauffé. Le procédé de chauffage d'air consiste à mélanger du carburant avec une partie d'air à chauffer en obtenant un mélange de carburant gazeux, effectuer son oxydation catalytique jusqu'à l'état de dioxyde de carbone, et mélanger les produits d'oxydation à la partie restante d'air chauffé. L'invention porte sur un dispositif pour mettre en oeuvre le procédé pour chauffer l'air et un procédé de régulation du chauffage d'air par variation d'amenée de carburant. Le mélange d'air et de carburant est obtenu avec un coefficient d'air prédéterminée par rapport au volume stœchiométrique et un chauffage préliminaire de celui-ci par une partie des produits d'oxydation. Le dispositif comprend une partie à échangeur de chaleur de chauffage d'air par les produits d'oxydation, ainsi que des soupapes montées sur la conduite d'alimentation en air du mélangeur de produits d'oxydation à de l'air, sur la conduite d'alimentation en carburant du mélangeur d'air et de carburant ainsi que sur une conduite de dérivation. La régulation la température de chauffage d'une partie de l'air par la variation de débit d'une parties des produits d'oxydation envoyée dans la partie à échangeur de chaleur, la régulation de la température maximale des produits d'oxydation par la variation du coefficient d'air en excès dans le mélange de combustible.
PCT/RU2013/000557 2012-07-03 2013-06-28 Procédé et régulation de chauffage d'air et dispositif de sa mise en oeuvre WO2014007679A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU2012128221/06A RU2499959C1 (ru) 2012-07-03 2012-07-03 Способ нагрева воздуха, устройство для его осуществления и способ регулирования нагрева воздуха
RU2012128221 2012-07-03

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Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2651916C1 (ru) * 2017-05-04 2018-04-24 Андрей Владиславович Курочкин Генератор горячего воздуха
RU2647940C1 (ru) * 2017-05-04 2018-03-21 федеральное государственное автономное образовательное учреждение высшего образования "Казанский (Приволжский) федеральный университет" (ФГАОУ ВО КФУ) Способ автоматической оптимизации процесса сжигания топлива переменного состава

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2133522A (en) * 1983-01-05 1984-07-25 Ross James Heaters Ltd Catalytic heating apparatus
RU2206835C2 (ru) * 2001-09-27 2003-06-20 Институт катализа им. Г.К. Борескова СО РАН Воздухонагреватель и способ его работы
RU2347977C1 (ru) * 2007-07-09 2009-02-27 Дмитрий Львович Астановский Способ сжигания топлива
WO2010074767A1 (fr) * 2008-12-26 2010-07-01 Vacca, Inc. Chauffage catalytique par jet en cavité
RU2444678C1 (ru) * 2011-03-14 2012-03-10 Дмитрий Львович Астановский Установка для сжигания топлива и нагрева технологических сред

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2145050C1 (ru) * 1998-06-01 2000-01-27 ООО "Теплосервис" Газовый воздухонагреватель
US6969506B2 (en) * 1999-08-17 2005-11-29 Battelle Memorial Institute Methods of conducting simultaneous exothermic and endothermic reactions
RU2306483C1 (ru) * 2006-05-06 2007-09-20 Открытое акционерное общество "Сибирский Агропромышленный Дом" (ОАО "САД") Способ сжигания жидкого или газообразного топлива для получения тепла и воздухонагреватель для его осуществления

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2133522A (en) * 1983-01-05 1984-07-25 Ross James Heaters Ltd Catalytic heating apparatus
RU2206835C2 (ru) * 2001-09-27 2003-06-20 Институт катализа им. Г.К. Борескова СО РАН Воздухонагреватель и способ его работы
RU2347977C1 (ru) * 2007-07-09 2009-02-27 Дмитрий Львович Астановский Способ сжигания топлива
WO2010074767A1 (fr) * 2008-12-26 2010-07-01 Vacca, Inc. Chauffage catalytique par jet en cavité
RU2444678C1 (ru) * 2011-03-14 2012-03-10 Дмитрий Львович Астановский Установка для сжигания топлива и нагрева технологических сред

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