EP1785685A1 - Dispositif et procédé pour chauffer des matériau de départ - Google Patents

Dispositif et procédé pour chauffer des matériau de départ Download PDF

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Publication number
EP1785685A1
EP1785685A1 EP05024539A EP05024539A EP1785685A1 EP 1785685 A1 EP1785685 A1 EP 1785685A1 EP 05024539 A EP05024539 A EP 05024539A EP 05024539 A EP05024539 A EP 05024539A EP 1785685 A1 EP1785685 A1 EP 1785685A1
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
anode
flue gas
petroleum coke
temperature
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP05024539A
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German (de)
English (en)
Inventor
Wolfgang Dr. Leisenberg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Innovatherm Prof Dr Leisenberg GmbH and Co KG
Original Assignee
Innovatherm Prof Dr Leisenberg GmbH and Co KG
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 Innovatherm Prof Dr Leisenberg GmbH and Co KG filed Critical Innovatherm Prof Dr Leisenberg GmbH and Co KG
Priority to EP05024539A priority Critical patent/EP1785685A1/fr
Priority to CA002564789A priority patent/CA2564789A1/fr
Priority to RU2006139439/02A priority patent/RU2006139439A/ru
Priority to US11/595,241 priority patent/US20070125316A1/en
Publication of EP1785685A1 publication Critical patent/EP1785685A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B13/00—Furnaces with both stationary charge and progression of heating, e.g. of ring type, of type in which segmental kiln moves over stationary charge
    • F27B13/06—Details, accessories, or equipment peculiar to furnaces of this type
    • F27B13/14—Arrangement of controlling, monitoring, alarm or like devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D19/00—Arrangements of controlling devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D19/00—Arrangements of controlling devices
    • F27D2019/0006—Monitoring the characteristics (composition, quantities, temperature, pressure) of at least one of the gases of the kiln atmosphere and using it as a controlling value
    • F27D2019/0018—Monitoring the temperature of the atmosphere of the kiln
    • F27D2019/0021—Monitoring the temperature of the exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D19/00—Arrangements of controlling devices
    • F27D2019/0028—Regulation
    • F27D2019/0031—Regulation through control of the flow of the exhaust gases

Definitions

  • the invention relates to a device, a control device and a method for heating a starting material, in particular of calcined petroleum coke, according to the features of the preambles of claims 1, 11 and 14.
  • anodes for fused-salt electrolysis for the production of primary aluminum are produced by the Hall-Heroult process in such a way that the starting material, in particular calcined petroleum coke, is fed to a mixing unit or kneader. Furthermore, a binder is added to the mixing unit.
  • the binder is usually coal tar pitch and is processed together with the calcined petroleum coke to a paste which is shaped as a so-called green anode and then fired in an anode ring furnace.
  • the anodes pass through three phases, namely a heating phase, a firing phase and a cooling phase. This is achieved by moving the suction, heating and cooling devices over the stationary anodes arranged in pits and sealed by the ambient air after a predetermined transfer cycle.
  • part of the waste heat arising in the cooling zone of the anode annealing furnace can be introduced into the supply line, through which the flue gas is sucked into the heat exchanger, by means of suction devices 4, the cooling of the anodes in the cooling zone is improved, since the heated one Air in the cooling zone is transported away faster. Furthermore, the temperature in the kiln hall drops because the extracted waste heat from the cooling zone no longer heats the immediate surroundings. This improves the working conditions in the area of the anode ring furnace.
  • the waste heat of an anode ring furnace 3 is to be made usable.
  • green anodes 4 are first heated to a certain temperature in a part of the furnace 3 functioning as a heating zone 22.
  • the introduced anodes 4 are exposed to an elevated temperature over a predetermined period of time.
  • the anodes 4 are cooled so that they can subsequently be used in an electrolytic cell to produce primary aluminum.
  • the temperature in the Bennzone 23 is achieved by means of burners 25, which are shown schematically.
  • the three zones 22, 23 and 24 are thermally connected to each other, so that the air heated at the hot anodes flows from the cooling zone 24 into the combustion zone 23 and finally into the heating zone 22 where it heats the introduced anodes 4.
  • the starting material for shaping the anode 4 is usually calcined petroleum coke 5 or 6, which is mixed in a defined manner from different grain fractions.
  • the calcined petroleum coke 5, 6 is fed by means of a binder 7, which consists of coal tar pitch 7, a mixing and shaping unit 8, in which the petroleum coke fractions. 5 and 6 and the binder 7 is processed into a paste and deformed to the green anode 4.
  • the device 1 it should be possible to use the waste heat arising in the anode ring furnace 3 for the heating of the petroleum coke 5 and 6.
  • the device 1 may comprise a plant part, through which the flue gas of the anode annealing furnace 3 pre-cleaned and cooled by a flue gas cleaning system is derived.
  • the extracted from the heating zone 22 flue gases are fed from a supply line 12 a heat exchanger 11.
  • the heat exchanger 11 of the calcined petroleum coke 5 and 6 is introduced and flows through the flue gas directly or flows around.
  • the heat exchanger 11 may have 5 or 6 individual units for the different petroleum coke fractions, in which the respective petroleum coke fractions 5 and 6 can be introduced.
  • the heat exchanger 11 is designed as a flow or moving bed heat exchanger, so that the introduced petroleum coke 5 or 6 at a certain speed pass through the heat exchanger 11 and are heated by the incoming flue gas.
  • the thus heated petroleum coke 5 or 6 is subsequently supplied to the mixing and forming unit 8, together with the binder 7, which is otherwise preheated the mixing and forming unit 8 is added.
  • the temperature difference between the heated petroleum coke 5 and 6 and the temperature of the effluent from the heat exchanger flue gas 13 is at least 50 K.
  • the controller 2 is electrically connected to a temperature sensor 19, through which the temperature of the heating zone 22 removed flue gas is measured. If the control device 2 determines that the temperature of the flue gas in the supply line 12 is too low, waste heat from it can be introduced into the supply line 12 via the throttle flap 29 of a suction device 31 which is connected to the cooling zone 24 of the anode ring furnace 3 , Since the supply line 12 is under negative pressure, fans are not required. Furthermore, the suction device 31 is connected via a further throttle valve 30 with the environment, so that optionally the cooling zone 24 removed waste heat with the Ambient air can be enriched to lower them to a certain predetermined temperature.
  • the flue gas in the supply line 12 can be further heated by a heating unit 20, which is also switched on or off by the control device 2.
  • a throttle valve 27 is provided, through which the access cross section of the supply line 12 into the heat exchanger 11 is controllable. Consequently, the amount of the flue gas portion flowing into the heat exchanger 11 can be regulated by the throttle valve 27. If only a partial flow of the flue gas is required for heating, the remainder is passed through a throttle flap 29 integrated in a bypass line 21, so that this flue gas flows directly from the feed line 12 around the heat exchanger 11.
  • the heat exchanger 11 is further connected to a discharge line 13, through which the exhaust gases of the flue gas cleaning system 14 are supplied.
  • the bypass line 21 opens into the discharge line 13, so that all the flue gases and the waste heat from the anode ring furnace 4 through the supply line 12 and the heat exchanger 11 in the discharge line 13 and thus in the flue gas cleaning system 14 or around the heat exchanger 11 through the bypass line 21 are led into the derivative 13.
  • the bypass line 21 can also open via a separate line 9 in a separate part of the flue gas cleaning system 14 in order to achieve a smaller pressure drop for the partial flow in the bypass line 21.
  • the temperature of the formed by the mixing and forming unit 8 anode 4 is about 160 ° C.
  • This temperature of the anode 4 is measured by a temperature sensor 19 and the temperature value of the finished shaped anode 4 is transmitted to the control device 2.
  • Further temperature sensors 19 measure the temperature of the petroleum coke 5 and 6 leaving the heat exchanger 11, as well as the petroleum cokes 5 and 6 to be introduced into the heat exchanger 11, and pass the thus measured temperature values to the control device 2. Due to the obtained temperature values of the petroleum cokes 5 and 6 and the finished shaped anode 4 can be determined by the control device 2, which temperature is required in the supply line 12 and the flaps 29, 30 of the suction device 4 set accordingly.
  • the burners 25 are reacted after a predetermined cycle, so that the former combustion zone 23 becomes the cooling zone 24.
  • the flue gas temperature which is passed through the supply line 12 in the heat exchanger 11 is lowest, but the temperature prevailing in the cooling zone 24 reaches its highest temperature level, a certain balance is already achieved by the opposite temperature profile, because the flue gas mixes with the waste heat removed from the cooling zone 24.
  • the exact required temperature in the supply line 12 is achieved by the control device 2 and by the position of the throttle valve 29 and optionally 30. Also, the maximum temperatures prevailing in the supply line 12 can be limited in this way.
  • the heating of the petroleum coke 5 and 6 is accomplished by the heating unit 20 integrated in the supply line 12.
  • the heat exchanger 11 Since the fumes pass through physical and chemical sorption processes when flowing through the petroleum coke 5 or 6 in the heat exchanger 11, the heat exchanger 11 already takes over a pre-separation function for the flue gas cleaning.
  • the flue gas cleaning system 14 fluidized bed reactor 15, which is operated depending on the requirements of the clean gases with special sorbents, such as ureas NH3 for the Nox deposition and / or activated carbon for the PAH separation and may optionally be designed as a multi-bed reactor, the flue gas is completely cleaned.
  • the fluid bed reactor 16, which is operated with limestone chippings, eliminates sulfur and fluorine residues from the flue gas.
  • the exemplary embodiment is based on an example of an energy balance, which is given below.
  • the ratio of anode mass flow and flue gas mass flow in the anode ring furnace 3 is due to the proportion of false air in the flue gas between 1: 3 and 1: 7 and on average about 1: 5.
  • the specific heats of petroleum coke 5 and 6 are about the same size, so that the flue gas mass flow as a multiple of the petroleum coke mass flow contains enough energy to heat the petroleum cokes 5 and 6.
  • the binder 7 is liquid at a temperature of about 200 ° C the starting material. So the petroleum coke fractions 5 and 6 mixed before their entry into the heat exchanger 11 and thus provides a portion of the required heating energy. Thus, a starting temperature of the petroleum coke 5 and 6 after the heat exchanger 11 of about 150 ° C is sufficient.
  • the temperature of the flue gas in the supply line 12 is affected by the number of fires traveling around the anode furnace 3 and varies between about 150 ° C to 250 ° C within one unit unpacking cycle. Since the temperature difference between the flue gas and the petroleum coke 5 and 6 at the output of the heat exchanger 11 should be about 50 K, it must be ensured that the temperature of the flue gas flowing into the heat exchanger 11, about 200 ° C. With these assumptions and a petroleum coke mass flow 5, 6 and the low green anode waste quantity 7 of 12, 5 t / h, a flue gas mass flow through the heat exchanger 11 of about 30 t / h is required. Since the flue gas mass flow in the supply line 12 is about 70 t / h with an average secondary air fraction, the part of about 40 t / h, which is not required for heating, is led past the heat exchanger 11 via the bypass line 21.
  • a triple-cascaded control with subordinate control is provided.
  • the temperature of the green anode 4 is measured as the main guide variable, that is, when the anode 4 leaves the mixing and shaping system 8.
  • the throttle valve 28 integrated in the bypass line 21 and the throttle valve 27, which is provided immediately before the heat exchanger 11 in the supply line 12, are adjusted in such a way by the control device 2 that by changing the flue gas volume flows in the heat exchanger 11 the desired petroleum coke outlet temperature is achieved.
  • This is expediently carried out by a cascade control with the coking temperature as auxiliary control variable.
  • the total mass flow of the flue gas is regulated by a throttle 30 connected to the environment such that the additional air taken from the cooling zone is minimized, i. only when the petroleum coke above the heating zone 22 exclusively removed flue gas temperature is no longer reached, in addition, the hot air from the cooling zone 24 can be added.
  • control device 2 Since the thermal processes take place relatively slowly, the control device 2 is subordinated to an adaptive control, which sets the control values of the individual throttle valves 27 to 30 in advance based on the empirical data of predetermined operating states and only slightly adjusts them by the control device 2 to the actual actual state Device 1 must be adjusted.
  • the control method according to the invention is preferably based on a neural network or a neuro-fuzzy algorithm.
EP05024539A 2005-11-10 2005-11-10 Dispositif et procédé pour chauffer des matériau de départ Withdrawn EP1785685A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP05024539A EP1785685A1 (fr) 2005-11-10 2005-11-10 Dispositif et procédé pour chauffer des matériau de départ
CA002564789A CA2564789A1 (fr) 2005-11-10 2006-10-20 Dispositif et procede de chauffage d'une matiere premiere
RU2006139439/02A RU2006139439A (ru) 2005-11-10 2006-11-09 Устройство и способ нагрева исходного материала
US11/595,241 US20070125316A1 (en) 2005-11-10 2006-11-09 Device and process for heating a primary material

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP05024539A EP1785685A1 (fr) 2005-11-10 2005-11-10 Dispositif et procédé pour chauffer des matériau de départ

Publications (1)

Publication Number Publication Date
EP1785685A1 true EP1785685A1 (fr) 2007-05-16

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EP05024539A Withdrawn EP1785685A1 (fr) 2005-11-10 2005-11-10 Dispositif et procédé pour chauffer des matériau de départ

Country Status (4)

Country Link
US (1) US20070125316A1 (fr)
EP (1) EP1785685A1 (fr)
CA (1) CA2564789A1 (fr)
RU (1) RU2006139439A (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009036799A1 (fr) * 2007-09-18 2009-03-26 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Procédé et dispositif de récupération de chaleur
WO2009046757A1 (fr) * 2007-10-08 2009-04-16 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Procédé et appareil d'exploitation de la chaleur résiduelle d'un four annulaire à anodes
CN101307985B (zh) * 2007-05-18 2010-12-01 贵州世纪天元矿业有限公司 一种煅烧方法及煅烧装置
WO2013044968A1 (fr) 2011-09-29 2013-04-04 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Procédé de surveillance
CN103160862A (zh) * 2011-12-14 2013-06-19 贵阳铝镁设计研究院有限公司 铝电解槽高浓度烟气经料箱的净化装置
WO2013110330A1 (fr) 2012-01-25 2013-08-01 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Procédé permettant de faire fonctionner un four de cuisson d'anodes et dispositif de commande
CN104748570A (zh) * 2015-04-10 2015-07-01 中国瑞林工程技术有限公司 一种利用空气冷却器热风的方法

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TR201904859T4 (tr) * 2011-03-29 2019-05-21 Kellog Co Isı geri kazanım sistemli fırın.
CN111748827A (zh) * 2020-07-29 2020-10-09 济南万瑞炭素有限责任公司 吸附沥青烟气粉回收及应用混捏的设备和工艺

Citations (3)

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US3173980A (en) * 1962-11-21 1965-03-16 Wheelabrator Corp Furnace dust and fume collection system
DE3013294A1 (de) * 1979-04-05 1980-10-23 Alusuisse Verfahren zum mischen und kuehlen von elektrodenmasse
DE3538151A1 (de) * 1985-10-26 1987-04-30 Schultze Rhonhof Ernst Dr Verfahren und vorrichtung zur herstellung von kunstkohlekoerpern

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US3703366A (en) * 1970-11-20 1972-11-21 John T Cullom Process for producing copper and elemental sulfur
DE2633789C3 (de) * 1976-07-28 1980-08-14 Wintershall Ag, 3100 Celle Verfahren und Vorrichtung zur Herstellung von Petrolkokskalzinat
US5012751A (en) * 1990-04-18 1991-05-07 Giant Resource Recovery Company, Inc. Process and apparatus for treating solid refuse
EP0529095B1 (fr) * 1991-03-02 1999-08-04 Sony Corporation Procédé pour la fabrication d'un matériau anodique et d'une cellule électrochimique non-aqueuse utilisant ce matériau
US6039791A (en) * 1997-10-23 2000-03-21 Kazeef; Michael G. Fused calcined petroleum coke and method of formation

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3173980A (en) * 1962-11-21 1965-03-16 Wheelabrator Corp Furnace dust and fume collection system
DE3013294A1 (de) * 1979-04-05 1980-10-23 Alusuisse Verfahren zum mischen und kuehlen von elektrodenmasse
DE3538151A1 (de) * 1985-10-26 1987-04-30 Schultze Rhonhof Ernst Dr Verfahren und vorrichtung zur herstellung von kunstkohlekoerpern

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101307985B (zh) * 2007-05-18 2010-12-01 贵州世纪天元矿业有限公司 一种煅烧方法及煅烧装置
WO2009036799A1 (fr) * 2007-09-18 2009-03-26 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Procédé et dispositif de récupération de chaleur
CN101606036B (zh) * 2007-09-18 2011-12-28 德国伊诺瓦有限公司 热量回收方法及设备
US8651856B2 (en) 2007-09-18 2014-02-18 Innovatherm Prof. Dr. Leisenberg Gmbh Method and device for heat recovery
WO2009046757A1 (fr) * 2007-10-08 2009-04-16 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Procédé et appareil d'exploitation de la chaleur résiduelle d'un four annulaire à anodes
WO2013044968A1 (fr) 2011-09-29 2013-04-04 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Procédé de surveillance
US9927175B2 (en) 2011-09-29 2018-03-27 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Monitoring method
CN103160862A (zh) * 2011-12-14 2013-06-19 贵阳铝镁设计研究院有限公司 铝电解槽高浓度烟气经料箱的净化装置
CN103160862B (zh) * 2011-12-14 2015-11-18 贵阳铝镁设计研究院有限公司 铝电解槽高浓度烟气经料箱的净化装置
WO2013110330A1 (fr) 2012-01-25 2013-08-01 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Procédé permettant de faire fonctionner un four de cuisson d'anodes et dispositif de commande
US9714791B2 (en) 2012-01-25 2017-07-25 Innovatherm Prof. Dr. Leisenberg Gmbh + Co. Kg Method for operating an anode furnace and control device
CN104748570A (zh) * 2015-04-10 2015-07-01 中国瑞林工程技术有限公司 一种利用空气冷却器热风的方法

Also Published As

Publication number Publication date
CA2564789A1 (fr) 2007-05-10
US20070125316A1 (en) 2007-06-07
RU2006139439A (ru) 2008-05-20

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