WO2002075003A2 - Argon oxygen decarburisation converter control method and system - Google Patents
Argon oxygen decarburisation converter control method and system Download PDFInfo
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- WO2002075003A2 WO2002075003A2 PCT/IT2002/000180 IT0200180W WO02075003A2 WO 2002075003 A2 WO2002075003 A2 WO 2002075003A2 IT 0200180 W IT0200180 W IT 0200180W WO 02075003 A2 WO02075003 A2 WO 02075003A2
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- oxygen
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
- C21C5/00—Manufacture of carbon-steel, e.g. plain mild steel, medium carbon steel or cast steel or stainless steel
- C21C5/28—Manufacture of steel in the converter
- C21C5/42—Constructional features of converters
- C21C5/46—Details or accessories
- C21C5/4673—Measuring and sampling devices
Definitions
- the present invention refers to a control method and to a related system for converters employed in stainless steelmaking, converters called AOD from Argon Oxygen
- the main goal in the AOD-type processes is to reach the end-point desirable in terms of Carbon as quickly as possible, fostering the oxidation of the Carbon in lieu of that of the Chromium without lowering the bath temperature below the optimum thermal level.
- the process times and the heat losses are decreased, but there is an increase in costs because of the need to add a reducing element (Silicon, Aluminium) in order to recover the Chromium oxide.
- the oxides resulting from the reduction of the Chromium oxide via the addition of said reducing agents increase the aggressiveness of the slag in relation to the refractory. In order to neutralise this effect, in a traditional process great quantities of lime are additioned, thereby increasing the thermal losses and the production costs.
- the best way to attain this aim is known to be an adequate lowering of the partial pressure of the Carbon monoxide (CO) in the liquid bath, lowering carried out by a controlled decrease of the Oxygen/inert gases ratio. In fact, this lowering fosters the oxidation of the Carbon, preventing an excessive oxidation of the Chromium.
- This lowering is usually carried out statically, i.e. the ratio is varied, at predetermined time intervals, of a discrete quantity.
- This system proved partly unsatisfactory since, though optimizing the process on the average, it fails to optimize the single casting.
- the technical problem underlying the present invention is to provide an AOD converter control method and system allowing to overcome the drawback mentioned with reference to the known art . This problem is solved by a method as abovespecified, comprising the following steps:
- a system as abovespecified comprises:
- a static control providing: the composition of the inletted ferrous metal; the desired steel type; the quantities of the additives to be additioned to the bath, and the initial values of the injected Oxygen and Nitrogen flow rates.
- the main advantage of the abovedefined method and system lies in ensuring the utmost effectiveness of the Oxygen blown into the converter and in letting the stainless steel refining process proceed at top speed.
- the present invention will hereinafter be described according to a preferred embodiment thereof, given by way of a non-limiting example with reference to the attached drawing, in which the sole figure schematically depicts an AOD converter.
- a base element of the system is an analyzer of the gases outletted from the converter 1, schematically indicated with 2 and located in the outlet duct 3 of the mouth 4 of the vessel 5.
- the probe of the waste gas analyzer (not shown) is positioned in the descending section of the outlet duct, upstream of the scrubber, in order to minimize the lag between the measuring of the gas composition and the actual gas composition at the outlet of the converter 1. Although thereat, the outletted gas has already mixed with the air inletted at the mouth 4, the measuring is sufficiently accurate.
- the model and the analyzer 2 interact therebetween by virtue of a control system implemented in a computer 6.
- the analyzer 2 is coupled to a flow rate meter, schematically indicated with 7 and it is positioned at a spot (not shown) downstream of the scrubber and upstream of the fans. This position prevents the probe 7 from being impinged onto by high-temperature and powder-rich gases .
- An adequate type of measuring system is an ultrasonic system consisting of a whirler (e.g. of the Vortex ® type) and a transducer. The temperature is measured in this same spot .
- the control system according to the present embodiment relies on the use of a mathematical model which simulates the performance of an AOD converter 1 (see figure) , thereby enabling the control system to select the optimum strategy .
- the model is designed to simulate: i) the converter startup; ii) the mass balance, to compute the bath composition due to the chemical reactions under way; iii) the energy balance, to compute the bath temperature due to the energy interactions; and iv) the variation of the operative conditions .
- hypotheses underlying the model can be summarized as follows : (a) the state variables of the converter assume the same value anywhere inside the vessel (perfect mixing hypothesis) ;
- the heat balance is performed by taking account of any loss (radiant energy, endothermal reduction reactions; blowing in of cold gases; addition of cold materials) .
- the chemical species reacting in the molten bath are: Iron (Fe) , Carbon (C) , Chromium (Cr) , Silicon (Si) , Nickel (Ni) and
- Manganese (Mn) Manganese
- composition of the gas blown in for the decarburization comprises Oxygen (0 2 ) , Argon (Ar) and
- Nitrogen (N 2 ) whereas the composition of the outletted gas additionally comprises Carbon monoxide (CO) .
- This model is employed to simulate the evolution of the decarburization process according to the base parameters (bath temperature, chemical composition) which vary according to the regulation variables (blowing parameters, additives) as well as to analyze the potential process evolution deriving from the different running strategies .
- the model is fed with other static data, like: the composition of the inletted ferrous metal, the temperature of the inletted material, the other features of the charged ferrous metal, the desired steel type.
- a static-type model provides several initial parameters: the quantities of the additives to be additioned to the bath and the initial values of the flow rates of Oxygen and Nitrogen injected via the nozzle 10 and the lance 11.
- the control system uses a proportional -type operation logic, simpler and more reliable than the systems which rely on a fuzzy control .
- the control method of the AOD converter 1 comprises a step of measuring the flow rate, the temperature and the composition of the gases outletted from the mouth 4 of the converter 1.
- the Oxygen/Inert gas ratio is varied (increased or decreased) , thereby keeping at all times the CRE (Carbon Removal Efficiency) above a critical threshold value depending on the steel type.
- the value of the critical CRE is computed in the light of the off-line simulations carried out with the mathematic model, whereas the CRE is computed with the measurings inputted by the field instruments: the %CO in the gases is multiplied by the flow rate of the waste gases (expressed in Nm 3 /min) and divided by the Oxygen flow rate .
- This system is calibrated so as to avoid eventual instabilities due to the lag between the instrument response and the adjusting actions.
- the application of the abovedescribed method and system yields a reduction in the consumption of Silicon in the order of 10%, with peaks of up to the 25%, and a reduction of the process times in the order of the 4%, with peaks of up to 16%.
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Carbon Steel Or Casting Steel Manufacturing (AREA)
- Control Of Non-Electrical Variables (AREA)
Abstract
AOD converter control system, based on the on-line analysis of the waste gases and on the processing thereof via a mathematical model which acts onto the flow rates of the process gases, so as to maximize the decarburization rate. This system comprises a waste gas analyzer (1), a flow rate meter (2), a control system based on a mathematical model which runs on a computer (3) and processes on-line the information outputted from said sensors, and a system for actuating the process gas valves (4).
Description
"AOD CONVERTER CONTROL METHOD AND SYSTEM"
DESCRIPTION
The present invention refers to a control method and to a related system for converters employed in stainless steelmaking, converters called AOD from Argon Oxygen
Decarburi zation .
In the AOD converters used for the refining of high Chromium stainless steels, the exact knowledge of the decarburization state is the key factor for an improved control of the blowing of the process gases. Most control systems apply static models in order to adjust the Oxygen/inert gases ratio at different predetermined steps, in some cases including a simulation carried out according to a dynamic model, yet lacking any process feedback [1-3] . However, these dynamic models for the AOD process, disclosed in the 70s by Asai and Szekely [4] , Fruehan [5] or Deb Roy and Robertson [6] , cannot simulate the decarburization as accurately as it is possible via the values measured from the composition and the flow rate of the waste gases [7, 8] .
The main goal in the AOD-type processes is to reach the end-point desirable in terms of Carbon as quickly as possible, fostering the oxidation of the Carbon in lieu of that of the Chromium without lowering the bath temperature below the optimum thermal level. In this way, the process times and the heat losses are decreased, but there is an increase in costs because of the need to add a reducing element (Silicon, Aluminium) in order to recover the Chromium oxide. Moreover, the oxides resulting from the reduction of the Chromium oxide via the addition of said reducing agents increase the aggressiveness of the slag in relation to the refractory. In order to neutralise this effect, in a traditional process great quantities of lime are additioned, thereby increasing the thermal losses and the production costs.
The best way to attain this aim is known to be an adequate lowering of the partial pressure of the Carbon
monoxide (CO) in the liquid bath, lowering carried out by a controlled decrease of the Oxygen/inert gases ratio. In fact, this lowering fosters the oxidation of the Carbon, preventing an excessive oxidation of the Chromium. This lowering is usually carried out statically, i.e. the ratio is varied, at predetermined time intervals, of a discrete quantity. This system proved partly unsatisfactory since, though optimizing the process on the average, it fails to optimize the single casting. The technical problem underlying the present invention is to provide an AOD converter control method and system allowing to overcome the drawback mentioned with reference to the known art . This problem is solved by a method as abovespecified, comprising the following steps:
* measuring the parameters related to the gases outletted from the mouth of the converter, in particular the flow rate, the temperature and the chemical composition; * processing said parameters according to a dynamic model ; and
* varying the ratio between Oxygen and inert gases blown in the converter so that the decarburization rate (dC/dt) is the maximum possible for the actual state of the steel-slag system.
According to the same inventive concept, a system as abovespecified comprises:
* a computer apt to store a dynamic model;
* an analyzer of the gases outletted from the converter, located in the outlet duct of the mouth and connected to said computer;
* a flow rate meter coupled to said analyzer; and
* a static control, providing: the composition of the inletted ferrous metal; the desired steel type; the quantities of the additives to be additioned to the bath, and the initial values of the injected Oxygen and Nitrogen flow rates.
The main advantage of the abovedefined method and system lies in ensuring the utmost effectiveness of the Oxygen blown into the converter and in letting the stainless steel refining process proceed at top speed. The present invention will hereinafter be described according to a preferred embodiment thereof, given by way of a non-limiting example with reference to the attached drawing, in which the sole figure schematically depicts an AOD converter. A base element of the system is an analyzer of the gases outletted from the converter 1, schematically indicated with 2 and located in the outlet duct 3 of the mouth 4 of the vessel 5. The probe of the waste gas analyzer (not shown) is positioned in the descending section of the outlet duct, upstream of the scrubber, in order to minimize the lag between the measuring of the gas composition and the actual gas composition at the outlet of the converter 1. Although thereat, the outletted gas has already mixed with the air inletted at the mouth 4, the measuring is sufficiently accurate.
The model and the analyzer 2 interact therebetween by virtue of a control system implemented in a computer 6. The analyzer 2 is coupled to a flow rate meter, schematically indicated with 7 and it is positioned at a spot (not shown) downstream of the scrubber and upstream of the fans. This position prevents the probe 7 from being impinged onto by high-temperature and powder-rich gases . An adequate type of measuring system is an ultrasonic system consisting of a whirler (e.g. of the Vortex® type) and a transducer. The temperature is measured in this same spot . The control system according to the present embodiment relies on the use of a mathematical model which simulates the performance of an AOD converter 1 (see figure) , thereby enabling the control system to select the optimum
strategy .
The model is designed to simulate: i) the converter startup; ii) the mass balance, to compute the bath composition due to the chemical reactions under way; iii) the energy balance, to compute the bath temperature due to the energy interactions; and iv) the variation of the operative conditions .
The hypotheses underlying the model can be summarized as follows : (a) the state variables of the converter assume the same value anywhere inside the vessel (perfect mixing hypothesis) ;
(b) the total Oxygen quantity injected is construed as completely reacted into the metallic phase; (c) the distribution of the Oxygen among the various metals depends on the respective oxidation rates; and
(d) during the blowing in of the Oxygen, the metal oxides are reduced by the Carbon present in the bath.
Moreover, the heat balance is performed by taking account of any loss (radiant energy, endothermal reduction reactions; blowing in of cold gases; addition of cold materials) .
In the present embodiment of the model, the chemical species reacting in the molten bath are: Iron (Fe) , Carbon (C) , Chromium (Cr) , Silicon (Si) , Nickel (Ni) and
Manganese (Mn) .
On the contrary, in the slag there are the following oxides: FeO, Cr304, Si02, NiO, MnO.
The composition of the gas blown in for the decarburization comprises Oxygen (02) , Argon (Ar) and
Nitrogen (N2) , whereas the composition of the outletted gas additionally comprises Carbon monoxide (CO) .
This model is employed to simulate the evolution of the decarburization process according to the base parameters (bath temperature, chemical composition) which vary according to the regulation variables (blowing parameters, additives) as well as to analyze the
potential process evolution deriving from the different running strategies .
Moreover, in the abovedescribed process the model is fed with other static data, like: the composition of the inletted ferrous metal, the temperature of the inletted material, the other features of the charged ferrous metal, the desired steel type. Further, a static-type model provides several initial parameters: the quantities of the additives to be additioned to the bath and the initial values of the flow rates of Oxygen and Nitrogen injected via the nozzle 10 and the lance 11. The control system uses a proportional -type operation logic, simpler and more reliable than the systems which rely on a fuzzy control . In the light of the abovedescribed system, the control method of the AOD converter 1 according to the present embodiment comprises a step of measuring the flow rate, the temperature and the composition of the gases outletted from the mouth 4 of the converter 1. According to the dynamic control and to the model fed to the computer 6 which works on the basis of the abovedescribed hypotheses, the Oxygen/Inert gas ratio is varied (increased or decreased) , thereby keeping at all times the CRE (Carbon Removal Efficiency) above a critical threshold value depending on the steel type. The value of the critical CRE is computed in the light of the off-line simulations carried out with the mathematic model, whereas the CRE is computed with the measurings inputted by the field instruments: the %CO in the gases is multiplied by the flow rate of the waste gases (expressed in Nm3/min) and divided by the Oxygen flow rate .
This system is calibrated so as to avoid eventual instabilities due to the lag between the instrument response and the adjusting actions.
The application of the abovedescribed method and system yields a reduction in the consumption of Silicon in the
order of 10%, with peaks of up to the 25%, and a reduction of the process times in the order of the 4%, with peaks of up to 16%.
A person skilled in the art, in order to meet further and contingent needs, may effect several further modifications and variants, to the abovedescribed control method and system, which however are all within the scope of the present invention, as defined by the appended claims . References
[1] Barilati, G. ; Di Sansebastiano, R. ; Moriondo, E.: Optimization of operation and metallurgical control of AOD by process automation. Iron and Steel Engineer, July 1990, p. 43-50 [2] Chiappero, A.; Barozzi, S.; Barilati, G. : A new high performance AOD converter.
2nd European Oxygen Steelmaking Congress, Taranto 1997, p. 121-133 [3] Lewis, D. A.; Pauley, D. E.; Rea, C; Shupay, M. E.; Naumann, J. D. : An on-line estimator expands automation of AOD. AISE Annual Convention, Pittsburgh 1998 [4] Asai, S.; Szekely. K. : Decarburization of Stainless Steel . Metallurgical Transactions 5 (1974), No. 3, p. 651- 657, No. 7, p. 1573-1580 [5] Fruehan, R. J. : Reaction model for the AOD Process.
Ironmaking and Steelmaking (1976), Nr. 3, p. 153-158 [6] Deb Roy, T.; Robertson, D. G. C: Mathematical model for stainless steelmaking.
Ironmaking and Steelmaking (1978), No. 5, p. 198-210 [7] Forster, D.; Mackenzie, K. ; Beeley, J. ; McVinnie, R. : Computerisation of AOD steelmaking at British Steel Stainless, Sheffield. 11th Process Technology Conference, Atlanta 1992, p. 3-8 [8] Kδhle, S.; Reichel, J. ; Kleimt, B.: Beobachtung des
Entkohlungsprozesses anhand von Abgasmessungen (Analysis of the decarburisation process on the basis of waste gas measurements) . Stahl u. Eisen 113 (1993) , No. 6, p. 55-60
Claims
1. An AOD converter control method comprises the following steps:
* measuring the parameters related to the gases outletted from the mouth (4) of the converter (1) , in particular the flow rate, the temperature and the chemical composition;
* processing said parameters according to a dynamic model ; and * varying the ratio between Oxygen and inert gases blown in the converter (1) so that at balance the Carbon content in the outletted gases follow a decarburization route which is related to the CRE (Carbon Removal Efficiency) actually implemented in the metallic bath rather than a preset one.
2. The method according to claim 1, wherein said model is based on the following hypotheses:
(a) the state variables of the converter assume the same value anywhere inside the vessel (perfect mixing hypothesis) ;
(b) the total Oxygen quantity injected is construed as completely reacted into the metallic phase;
(c) the distribution of the Oxygen among the various metals depends on the respective oxidation rates; and (d) during the blowing in of the Oxygen, the metal oxides are reduced by the Carbon present in the bath.
3. The method according to claim 2, wherein in said model the chemical species reacting in the molten bath are: Iron (Fe) , Carbon (C) , Chromium (Cr) , Silicon (Si), Nickel (Ni) and Manganese (Mn) .
4. The method according to claim 2, wherein in said model in the slag there are the following oxides: FeO, Cr304 Si02, NiO, MnO.
5. The method according to claim 2 , wherein in said model the composition of the gas blown in for the decarburization comprises Oxygen (02) , Argon (Ar) and Nitrogen (N2) .
6. The method according to claim 2 , wherein in said model the composition of the outletted gas comprises Oxygen (02) , Argon (Ar) , Nitrogen (N2) and Carbon monoxide (CO) .
7. The method according to claim 2, wherein the model is designed according to a proportional logic.
8. An AOD converter control system for implementing the method according to one of the preceding claims, comprising: * a computer (6) apt to store a dynamic model;
* an analyzer (2) of the gases outletted from the converter (1) located in the outlet duct (3) of the mouth (4) and connected to said computer (6) ;
* a flow rate meter (7) coupled to said analyzer (2) ; and
* a static control, providing: the composition of the inletted ferrous metal; the desired steel type; the quantities of the additives to be additioned to the bath, and the initial values of the injected Oxygen and Nitrogen.
9. The system according to claim 8, wherein the analyzer (2) is positioned in the descending section of the outlet duct (3) , optionally upstream of the scrubber.
10. The system according to claim 8, wherein the flow rate meter (7) is positioned downstream of the scrubber, optionally upstream of the fans.
11. The system according to claim 10, wherein the flow rate meter (7) is of ultrasonic type and it comprises a whirler and a transducer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2002253520A AU2002253520A1 (en) | 2001-03-21 | 2002-03-21 | Argon oxygen decarburisation converter control method and system |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ITRM2001A000146 | 2001-03-21 | ||
| IT2001RM000146A ITRM20010146A1 (en) | 2001-03-21 | 2001-03-21 | METHOD AND CONTROL SYSTEM FOR AOD CONVERTERS. |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2002075003A2 true WO2002075003A2 (en) | 2002-09-26 |
| WO2002075003A3 WO2002075003A3 (en) | 2003-02-13 |
Family
ID=11455351
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/IT2002/000180 Ceased WO2002075003A2 (en) | 2001-03-21 | 2002-03-21 | Argon oxygen decarburisation converter control method and system |
Country Status (3)
| Country | Link |
|---|---|
| AU (1) | AU2002253520A1 (en) |
| IT (1) | ITRM20010146A1 (en) |
| WO (1) | WO2002075003A2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008049673A1 (en) * | 2006-10-27 | 2008-05-02 | Siemens Aktiengesellschaft | Method of regulating the output of carbon monoxide in a metallurgical melting process |
| US8048196B2 (en) | 2006-11-30 | 2011-11-01 | Sms Siemag Aktiengesellschaft | Method and device for producing stainless steel without using a supply of electrical energy, based on pig-iron that has been pre-treated in a DDD installation |
| US8430945B2 (en) | 2006-11-30 | 2013-04-30 | Sms Siemag Aktiengesellschaft | Method and device for producing pig-iron based stainless steel without using a supply of electrical energy |
| JP2013181194A (en) * | 2012-03-01 | 2013-09-12 | Jfe Steel Corp | Support method for blowing process operation and support device for blowing process operation |
| CN103805733A (en) * | 2002-11-16 | 2014-05-21 | Sms西马格股份公司 | Gas supply system for a metallurgical furnace and operating method for said system |
| CN105750292A (en) * | 2016-04-28 | 2016-07-13 | 无锡三达环保科技有限公司 | Ladle detaching capturing hood for AOD furnace |
| CN109811136A (en) * | 2019-01-11 | 2019-05-28 | 东北大学 | A kind of slag bath carbon thermal reduction slag bath compensation method for thermal |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3594155A (en) * | 1968-10-30 | 1971-07-20 | Allegheny Ludlum Steel | Method for dynamically controlling decarburization of steel |
| US3816720A (en) * | 1971-11-01 | 1974-06-11 | Union Carbide Corp | Process for the decarburization of molten metal |
| US3920447A (en) * | 1972-02-28 | 1975-11-18 | Pennsylvania Engineering Corp | Steel production method |
| JPS5131001B2 (en) * | 1972-10-18 | 1976-09-04 | ||
| JPS5938316A (en) * | 1982-08-25 | 1984-03-02 | Kawasaki Steel Corp | Production of high chromium steel |
| SE452475B (en) * | 1983-03-21 | 1987-11-30 | Nippon Yakin Kogyo Co Ltd | PROCEDURE FOR COMPUTER CONTROLLED COOLING OF A STEEL MELT |
-
2001
- 2001-03-21 IT IT2001RM000146A patent/ITRM20010146A1/en unknown
-
2002
- 2002-03-21 WO PCT/IT2002/000180 patent/WO2002075003A2/en not_active Ceased
- 2002-03-21 AU AU2002253520A patent/AU2002253520A1/en not_active Abandoned
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103805733A (en) * | 2002-11-16 | 2014-05-21 | Sms西马格股份公司 | Gas supply system for a metallurgical furnace and operating method for said system |
| WO2008049673A1 (en) * | 2006-10-27 | 2008-05-02 | Siemens Aktiengesellschaft | Method of regulating the output of carbon monoxide in a metallurgical melting process |
| US8092572B2 (en) | 2006-10-27 | 2012-01-10 | Siemens Aktiengesellschaft | Method of regulating the output of carbon monoxide in a metallurgical melting process |
| RU2454465C2 (en) * | 2006-10-27 | 2012-06-27 | Сименс Акциенгезелльшафт | Control method of carbon oxide discharge during metallurgical melting process |
| US8048196B2 (en) | 2006-11-30 | 2011-11-01 | Sms Siemag Aktiengesellschaft | Method and device for producing stainless steel without using a supply of electrical energy, based on pig-iron that has been pre-treated in a DDD installation |
| US8425831B2 (en) | 2006-11-30 | 2013-04-23 | Sms Siemag Aktiengesellschaft | Method and device for producing stainless steel without using a supply of electrical energy, based on pig-iron that has been pre-treated in a DDD installation |
| US8430945B2 (en) | 2006-11-30 | 2013-04-30 | Sms Siemag Aktiengesellschaft | Method and device for producing pig-iron based stainless steel without using a supply of electrical energy |
| US8765051B2 (en) | 2006-11-30 | 2014-07-01 | Sms Siemag Aktiengesellschaft | Method and device for producing pig-iron based stainless steel without using a supply of electrical energy |
| JP2013181194A (en) * | 2012-03-01 | 2013-09-12 | Jfe Steel Corp | Support method for blowing process operation and support device for blowing process operation |
| CN105750292A (en) * | 2016-04-28 | 2016-07-13 | 无锡三达环保科技有限公司 | Ladle detaching capturing hood for AOD furnace |
| CN109811136A (en) * | 2019-01-11 | 2019-05-28 | 东北大学 | A kind of slag bath carbon thermal reduction slag bath compensation method for thermal |
| CN109811136B (en) * | 2019-01-11 | 2020-06-02 | 东北大学 | Slag bath carbon thermal reduction slag bath thermal compensation method |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2002253520A1 (en) | 2002-10-03 |
| ITRM20010146A0 (en) | 2001-03-21 |
| ITRM20010146A1 (en) | 2002-09-21 |
| WO2002075003A3 (en) | 2003-02-13 |
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