EP0201438B1 - Verfahren zur genauen Regulierung einer geringen Tonerdegehalts in einer schmelzflüssigen Elektrolysezelle zur Aluminiumherstellung - Google Patents

Verfahren zur genauen Regulierung einer geringen Tonerdegehalts in einer schmelzflüssigen Elektrolysezelle zur Aluminiumherstellung Download PDF

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Publication number
EP0201438B1
EP0201438B1 EP86420118A EP86420118A EP0201438B1 EP 0201438 B1 EP0201438 B1 EP 0201438B1 EP 86420118 A EP86420118 A EP 86420118A EP 86420118 A EP86420118 A EP 86420118A EP 0201438 B1 EP0201438 B1 EP 0201438B1
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Prior art keywords
alumina
rate
electrolysis
cell
bath
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Expired
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EP86420118A
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English (en)
French (fr)
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EP0201438A1 (de
Inventor
Michel Leroy
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Rio Tinto France SAS
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Aluminium Pechiney SA
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Priority to AT86420118T priority Critical patent/ATE44165T1/de
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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
    • C25C3/06—Electrolytic production, recovery or refining of metals by electrolysis of melts of aluminium
    • C25C3/20—Automatic control or regulation of cells

Definitions

  • the present invention relates to a process for the precise regulation of a low alumina content in an igneous electrolysis tank for the production of aluminum according to the Hall-Héroult process, this regulation also having the aim of maintaining the Faraday yield at a level high, at least equal to 94%.
  • This parameter is generally the variation of the internal resistance, or, more exactly, of the internal pseudo-resistance which is equal to:
  • Eo being an image of the counter-electromotive force of the tank, the value of which is generally assumed to be 1.65 volts, U the voltage across the terminals of the tank and J the intensity passing through it.
  • the alumina concentration is fixed in the range of 2 to 8%.
  • the disadvantage of this process is that its sensitivity varies with the alumina content, which is precisely minimal in the interval used, from 3 to 5% of A1 2 0 3 (table p. 8).
  • the alumina content is also fixed in the range of 2 to 8% and, preferably, 4 to 6%.
  • the tank is fed for a predetermined time t with an amount of alumina higher than its theoretical consumption, until a predetermined alumina concentration is obtained (for example up to 7%), then the supply is switched to a rate equal to the theoretical consumption for a predetermined time t 2 , then the feeding is stopped until the appearance of the first symptoms of anode effect ("packaging"), and the feeding cycle is resumed at a rate which is greater than the theoretical consumption.
  • the alumina concentration varies, during the cycle, from 4.9 to 8% (example 1) or from 4.0 to 7% (example 2).
  • slope calculation is based on successive measurements of the internal resistance R;, at equal time intervals, on the evaluation of the slope dRi / dt of variation of R i as a function of time, and the comparison of R i on the one hand and of dRi / dt on the other hand, to set values, and on the modification of the rate of introduction of alumina, so as to reduce dRi / dt and R i at setpoint values.
  • the search for the optimal operating mode that is to say the search for the operating parameters of the electrolytic cells giving the best cost price, or the biggest profit margin for a given investment, has always been a permanent concern. for those skilled in the art.
  • the object of the invention is an improvement of the process for the precise regulation of a low alumina content in the electrolysis tank, making it possible to significantly improve the Faraday yield.
  • Energy consumption per tonne of aluminum produced can depend on the yield Faraday, F, and the voltage across a tank, U, in the form:
  • this optimal alumina content is very close to the minimum content below which appears the "anode effect", also called “packaging” or “polarization” , which results in a very sharp rise in the voltage across the cell and in the temperature of the electrolysis bath, and in the release in significant quantities of fluorinated products from the decomposition of the electrolysis bath.
  • the object of the invention is therefore to provide such a process for regulating the alumina content of the bath in the low content range, by the use of a synthetic parameter P which can be calculated simply from conventional measurements made on a tank.
  • electrolysis namely: the voltage at the terminals of each cell, the intensity traversing the file of cells and the rate of supply of alumina (in kg / hour for example).
  • CN being the nominal rate of supply of alumina and C- the rate of undernourishment, counted in kg of alumina per unit of time, Q (AI 2 0 3 ) being the quantity of alumina consumed by the tank in the same time unit and
  • the parameter P is evaluated from the internal pseudo-resistance of the tank, R;, itself defined by:
  • Eo is a standard value, in volts, of the dynamic counter-electromotive force of the tank, generally between 1.5 and 2.0 volts, and most often of the order of 1.65 to 1.75 volts
  • R i is then expressed in microohms;
  • D is the alumina content drift of the electrolysis bath, expressed in weight percent per hour
  • P is expressed by the formula: (P being expressed in microohms per second and per% weight per hour).
  • This initial period which generally lasts only a few minutes, corresponds to the end of dissolution of the excess alumina introduced during the overeating period and not immediately assimilated by the bath.
  • Another method is to add a period of a few minutes at nominal rate after overeating before going on to undereating.
  • the alumina content of the bath decreases all the faster the slower the feed rate, and, in parallel, the measured slope dR; / dt increases.
  • the alumina content drift, D, counted in% weight per hour, is then proportional to:
  • C- is the rate of undernourishment counted in kg of A1 2 0 3 introduced per second and C N is the nominal rate of feed (counted in the same units).
  • Any other coherent system of units can of course be used, for example the inverse of the time separating the introduction of 2 consecutive doses of alumina.
  • Q (Al 2 O 3 ) is the weight of alumina consumed per unit of time, by electrolysis.
  • Q (bl) is the weight of liquid bath, capable of dissolving alumina, contained in the crucible of the tank (for information, if the weight of liquid bath is measured in kg, of the order of 30 J where J is the electrolysis intensity counted in kA): note that the time constant for the melting or solidification of the bath at the slope is very large (generally of the order of several hours), this quantity only varies very slowly over time.
  • the targeted alumina content being close to the limit content triggering the appearance of a polarization of the tank, it is essential that after operation at nominal rate, the readjustment is done by preceding the search phase of the operating point (characterized by Po), during an under-timing, by a period of over-timing which allows s '' move away from this limit content before starting the search.
  • Po search phase of the operating point
  • the regulation method according to the invention can be used only during part of the operating time of the tank, and preferably when the tank is stable.
  • this parameter Po will be maintained between the limit values of 2/100 J and 10/100 J.
  • K I and K 2 The estimation of K I and K 2 can be done as follows:
  • the economic coefficient K I summarizes the economic conditions of the moment. It is substantially equal to the ratio of the sum of the fixed transformation costs (excluding alumina), including in particular the cost of energy and consumable carbon products, labor and depreciation, including financial costs, at cost Energy.
  • K I is approximately equal to: (an estimate of K 1 at ⁇ 20% is more than enough to get close enough to the economic optimum).
  • the "technical” coefficient K 2 summarizes the technological and physicochemical characteristics of the tank and can be evaluated as follows:
  • F is the Faraday yield of the tank, generally between 0.88 and 0.96 for these same properly conducted tanks
  • dF / d (AI 2 0 3 ) is the algebraic drift of the Faraday yield relative to the alumina content of the bath , counted as a% of Faraday per% of alumina, in the region of alumina contents between 1% and 4%, and preferably in the region of A1 2 0 3 contents between 1.5% and 3%.
  • this factor dF / d (Al 2 O 3 ) must be determined experimentally for each type of tank and for the various types of bath used (low acid baths, with less than 8% excess of AIF 3 , or very acid baths, with more than 8% excess of AIF 3 or with sub-additives such as LiF and MgF 2 ). Once determined, it no longer depends, as a first approximation, on economic conditions.
  • the invention was applied to a series of electrolysis cells operating at an intensity of 280 KA, at a voltage of 4.10 volts per cell and giving a Faraday yield of 95.0% for an average alumina content in the bath. electrolysis equal to 2.3%, previously regulated according to the method of our patent FR-2 487 386 already cited (process called "slope calculation").
  • the daily production of the series per tank was 2.145 kg / day, for an energy consumption of 12.860 kWh / ton.
  • the gain on the cost price was 20 F per tonne of aluminum produced.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Electrolytic Production Of Metals (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Cell Separators (AREA)
  • Investigating Or Analysing Materials By Optical Means (AREA)
  • Electrical Discharge Machining, Electrochemical Machining, And Combined Machining (AREA)
  • Diaphragms For Electromechanical Transducers (AREA)
  • Weting (AREA)
  • Table Devices Or Equipment (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Claims (8)

1. Verfahren zur genauen Regulierung eines geringen Tonerdegehaltes im Bereich von 1 bis 3 % in einer Zelle zur Aluminiumerzeugung durch Elektrolyse nach dem Hall-Heroult-Verfahren, das das Erhalten eines Faraday-Ausbringens von wenigstens gleich 94 % ermöglicht, indem man eine Wechselfolge von Perioden einer Speisung der Elektrolysezelle mit Tonerde in einem Nenntakt CN, einem verringerten Takt C- und einem Takt C+ über dem Nenntakt anwendet, welches Verfahren zunächst darin besteht, einen Regulierungsparameter P = -1/D (dRi/dt) zu bestimmen, der in Mikroohm je Sekunde und durch Gew.-% je Stunde ausgedrückt wird, wobei di der Innenwiderstand der Zelle und t die Zeit ist, Die die Ableitung des Gehalts des Elektrolysebades an Tonerde, der in Gew.-% je Stunde ausgedrückt wird, nach der Beziehung
Figure imgb0016
CN der Nenntakt der Speisung mit Tonerde und C- der Unterspeisungstakt ist, die als kg Tonerde je Zeiteinheit gerechnet werden, Q(Al2O3) die durch die Zelle in der gleichen Zeiteinheit verbrauchte Tonerdemenge ist und Q. (b.l.) die in der Zelle enthaltene flüssige Elektrolysebadmenge ist und das Verfahren anschließend darin besteht, wiederholt die folgenden Schritte durchzuführen:
a) man speist die Zelle im Nenntakt CN (derart, daß die in das Bad eingeführte Tonerdemenge genau gleich der durch die Elektrolyse verbrauchten Menge ist);
b) man setzt periodisch eine Überspeisung mit Tonerde in einem Takt C+ über dem Nenntakt CN derart, daß das Bad an Tonerde angereichert wird, und während einer vorbestimmten Dauer t+ in Gang. Während dieser Periode ist dRi/dt negativ;
c) man geht zur Unterspeisung, d. h. zu einem Takt C- unter CN über. Die Neigung dRi/dt verschwindet und wird dann positiv. Man mißt häufig den Regulierungsparameter P, dessen Wert zum Wachsen neigt;
d) man vergleicht die aufeinanderfolgenden Werte von P mit einem vorbestimmten Einstellwert Po. Sobald P = Po, geht man wieder zum Nennspeisungstakt CN über und beginnt wieder einen neuen Zyklus bei a).
2. Regulierungsverfahren nach Anspruch 1,
dadurch gekennzeichnet,
daß man nach dem Überspeisungsschritt b) während einiger Minuten zum Nenntakt CN übergeht, bevor man zur Unterspeisung übergeht.
3. Regulierungsverfahren nach Anspruch 1, dadurch gekennzeichnet, daß man nach dem Uberspeisungsschritt b) während einiger Minuten zu einem von CN wenig verschiedenen Takt übergeht.
4. Regulierungsverfahren nach Anspruch 1,
dadurch gekennzeichnet,
daß der Einstellwert Po des Regulierungsparameters P auf Basis der Stärke J in kA des Elektrolysestroms und zweier Koeffizienten K1, der mit den Produktionskosten verknüpft ist, und K2, der mit den physikochemischen Eigenschaften der Zelle verknüpft ist, entsprechend der Beziehung Po = K1 K2/J bestimmt wird.
5. Regulierungsverfahren nach Anspruch 4,
dadurch gekennzeichnet,
daß der Koeffizient K1 genau gleich dem Verhältnis der Summe der festen Umwandlungskosten (Energie, verbrauchbare Kohlenstoffprodukte, Arbeitskosten, Amortisationen) zu den Kosten der elektrischen Energie ist.
6. Regulierungsverfahren nach Anspruch 4, dadurch gekennzeichnet, daß der Koeffizient K2 genau gleich:
Figure imgb0017
7. Regulierungsverfahren nach irgendeinem der Ansprüche 1 bis 4,
dadurch gekennzeichnet,
daß der Einstellwert Po des Regulierungsparameters P, ausgedrückt in Mikroohm je Sekunde und durch Gew.-% je Stunde, zwischen 2/100 J und 10/100 . J festgelegt wird, wobei die Stärke J des Elektrolysestroms in kA ausgedrückt wird.
EP86420118A 1985-05-07 1986-05-05 Verfahren zur genauen Regulierung einer geringen Tonerdegehalts in einer schmelzflüssigen Elektrolysezelle zur Aluminiumherstellung Expired EP0201438B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT86420118T ATE44165T1 (de) 1985-05-07 1986-05-05 Verfahren zur genauen regulierung einer geringen tonerdegehalts in einer schmelzfluessigen elektrolysezelle zur aluminiumherstellung.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8507319A FR2581660B1 (fr) 1985-05-07 1985-05-07 Procede de regulation precise d'une faible teneur en alumine dans une cuve d'electrolyse ignee pour la production d'aluminium
FR8507319 1985-05-07

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EP0201438A1 EP0201438A1 (de) 1986-11-12
EP0201438B1 true EP0201438B1 (de) 1989-06-21

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US (1) US4654129A (de)
EP (1) EP0201438B1 (de)
JP (1) JPS61261490A (de)
CN (1) CN1006307B (de)
AT (1) ATE44165T1 (de)
AU (1) AU576152B2 (de)
BR (1) BR8602039A (de)
CA (1) CA1251417A (de)
DE (1) DE3664058D1 (de)
ES (1) ES8800733A1 (de)
FR (1) FR2581660B1 (de)
GR (1) GR861139B (de)
HU (1) HU205632B (de)
IN (1) IN164906B (de)
IS (1) IS1347B6 (de)
MY (1) MY101644A (de)
NO (1) NO172192C (de)
NZ (1) NZ216051A (de)
OA (1) OA08324A (de)
PL (1) PL144950B1 (de)
TR (1) TR22683A (de)
ZA (1) ZA863380B (de)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2605410B1 (fr) * 1986-10-17 1988-11-25 Pechiney Aluminium Procede et dispositif de mesure electrochimique de la concentration en ions oxyde dans un bain a base d'halogenures fondus
CA2010322C (en) 1989-02-24 1998-08-18 Geoffrey I. Blatch Process for controlling aluminium smelting cells
DE59105830D1 (de) * 1990-05-04 1995-08-03 Alusuisse Lonza Services Ag Regulierung und Stabilisierung des A1F3-Gehaltes in einer Aluminiumelektrolysezelle.
ZA915511B (en) * 1990-07-17 1992-04-29 Commw Scient Ind Res Org Rock bolt system and method of rock bolting
FR2749858B1 (fr) * 1996-06-17 1998-07-24 Pechiney Aluminium Procede de regulation de la teneur en alumine du bain des cuves d'electrolyse pour la production d'aluminium
CA2230882C (en) 1997-03-14 2004-08-17 Dubai Aluminium Company Limited Intelligent control of aluminium reduction cells using predictive and pattern recognition techniques
NO311623B1 (no) * 1998-03-23 2001-12-17 Norsk Hydro As Fremgangsmåte for styring av aluminiumoksidtilförsel til elektrolyseceller for fremstilling av aluminium
FR2821364B1 (fr) 2001-02-28 2004-04-09 Pechiney Aluminium Procede de regulation d'une cellule d'electrolyse
US6837982B2 (en) 2002-01-25 2005-01-04 Northwest Aluminum Technologies Maintaining molten salt electrolyte concentration in aluminum-producing electrolytic cell
CA2671066C (en) * 2006-12-19 2016-07-26 Michael Schneller Aluminum production process control
EP2135975A1 (de) 2008-06-16 2009-12-23 Alcan International Limited Verfahren zur Herstellung von Aluminium in einer Elektrolysezelle

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3629079A (en) * 1968-02-23 1971-12-21 Kaiser Aluminium Chem Corp Alumina feed control
US3712857A (en) * 1968-05-20 1973-01-23 Reynolds Metals Co Method for controlling a reduction cell
US3622475A (en) * 1968-08-21 1971-11-23 Reynolds Metals Co Reduction cell control system
FR2487386A1 (fr) * 1980-07-23 1982-01-29 Pechiney Aluminium Procede et appareillage pour reguler de facon precise la cadence d'introduction et la teneur en alumine d'une cuve d'electrolyse ignee, et application a la production d'aluminium
US4425201A (en) * 1982-01-27 1984-01-10 Reynolds Metals Company Method for improved alumina control in aluminum electrolytic cells
NO166821C (no) * 1985-02-21 1991-09-04 Aardal & Sunndal Verk As Fremgangsmaate for styring av aluminiumoksyd-tilfoerselen til elektrolyseovner for fremstilling av aluminium.

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IN164906B (de) 1989-07-01
HUT45102A (en) 1988-05-30
AU5715786A (en) 1986-11-13
ES8800733A1 (es) 1987-11-16
TR22683A (tr) 1988-03-03
OA08324A (fr) 1988-02-29
ZA863380B (en) 1987-02-25
NO172192C (no) 1993-06-16
IS3095A7 (is) 1986-11-08
FR2581660B1 (fr) 1987-06-05
DE3664058D1 (en) 1989-07-27
HU205632B (en) 1992-05-28
JPS61261490A (ja) 1986-11-19
AU576152B2 (en) 1988-08-11
GR861139B (en) 1986-08-21
EP0201438A1 (de) 1986-11-12
NO172192B (no) 1993-03-08
IS1347B6 (is) 1989-03-20
PL144950B1 (en) 1988-07-30
CA1251417A (fr) 1989-03-21
NZ216051A (en) 1989-10-27
CN1006307B (zh) 1990-01-03
ES554683A0 (es) 1987-11-16
US4654129A (en) 1987-03-31
ATE44165T1 (de) 1989-07-15
FR2581660A1 (fr) 1986-11-14
MY101644A (en) 1991-12-31
CN86103165A (zh) 1986-11-05
BR8602039A (pt) 1987-01-06
NO861806L (no) 1986-11-10

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