USRE19770E - Production of sponge ibxn - Google Patents
Production of sponge ibxn Download PDFInfo
- Publication number
- USRE19770E USRE19770E US19770DE USRE19770E US RE19770 E USRE19770 E US RE19770E US 19770D E US19770D E US 19770DE US RE19770 E USRE19770 E US RE19770E
- Authority
- US
- United States
- Prior art keywords
- gas
- heat
- air
- reduction
- reducing
- 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.)
- Expired
Links
- 238000004519 manufacturing process Methods 0.000 title description 2
- 239000007789 gas Substances 0.000 description 31
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 23
- 150000002430 hydrocarbons Chemical class 0.000 description 20
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 14
- 239000004215 Carbon black (E152) Substances 0.000 description 11
- 229910052742 iron Inorganic materials 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 10
- 229910052799 carbon Inorganic materials 0.000 description 8
- 229910002091 carbon monoxide Inorganic materials 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 8
- 239000001257 hydrogen Substances 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- SZVJSHCCFOBDDC-UHFFFAOYSA-N Iron(II,III) oxide Chemical compound O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 239000003345 natural gas Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 239000002912 waste gas Substances 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- KBJMLQFLOWQJNF-UHFFFAOYSA-N Nickel(II) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 229910000460 iron oxide Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UHOVQNZJYSORNB-UHFFFAOYSA-N benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000003197 catalytic Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000002480 mineral oil Substances 0.000 description 1
- 235000010446 mineral oil Nutrition 0.000 description 1
- -1 natural gas Chemical class 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
- C21B13/146—Multi-step reduction without melting
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
Definitions
- the hydrocarbons are rst converted to a reducing gas consisting of a mixture of hydrogen and carbon monoxide.
- the conversion is accomplished by passing the hydrocarbon, such as natural gas, with a certain quantity of air through a catalytic chamber.
- a catalytic chamber is filled with particles of firebrick, coke or graphite or a mixture of one or more, some of which have been dipped in a solution of nickel nitrate, dried and ignited.
- the quantityof air should be such that the oxygen contained therein is Just suiilcient to combine with the carbon of the hydrocarbon to form carbon monoxide, liberating the hydrogen.
- the reaction of conversion of hydrocarbons with air to carbon monoxide and hydrogen is exothermic, but some hydrocarbons. such as natural gas do not produce sufficient heat to raise thegas to the high temperature desired (2000 FJ; consequently it is necessary to sup ply heat to the reaction.
- This heat may be supplied in various ways; as, for example, by passing an electric current through the catalyzer, or heat may be transferred through oven walls, or heat may be supplied by using intermittently two or more stoves in the usual manner.
- hydrocarbon compounds of carbon and hydrogen.
- natural gas which is a mixture of methane, ethane, and higher members of the series such as propane.
- any volatile hydrocarbon such as mineral oil or benzol may be used.
- the hydrocarbons containing a high percentage of carbon it may not be necessary to heat the generator.
- coke oven gas containing a mixture of hydrogen, carbon oxides and hydrocarbons can be used in place of natural gas.
- a particular process embodying the invention is the following: A mixture of air and natural l5 gas is passed through a chamber containing a cataiyzer, consisting of pieces of coke or graphite which have been dipped in a solution of nickel nitrate, dried and ignited. A current of electricity is passed through the chamber, thus 20 supplying the heat required. Both the air and the natural gas have been heated (to 1500- 1000 respectively), by passing counter-current with the waste gas from reduction through heat exchangers. On accolmt of the preheat, the 25 heat required to be supplied by electricity is not excessive. v
- the reduction gas so produced at 2000" F. is conveyed to the reducing chamber. While I do not desire to limit the iorm or design of the 30 reducing chamber or chambers, I describe the following as a practicable arrangement. Reduction is accomplished in two chambers. The large part of the reduction is accomplished in a kiln and the nal reduction is accomplished in 35 a shaft. The partially reduced material from the kiln empties into the shaft. 'I'he reducing gas enters near the bottom of the shaft and extends upwards, reducing all but trace of any iron oxide remaining. I'he gases then pass into the 40 kiln where the main part of the reduction occurs. The gas ilrst reduces the bulk oi' the FeO to Fe and then passing on reduces the FeaO: to FeO. i i
- the gas which is bled containing as it does both sensible heat (temperature 1600*' F.) and heat of combustion, may be used for other purposes, but half of it, or 40 per cent oi' the entire gas after reduction, may be used to heat the generator unless the generator is heated electrically.
- the waste gases pass through a heat exchanger, counter-current to air. 'Ihis air is later used in the generator.
- This heat exchanger is so constructed that the cold air passes through the cold part of the exchanger then passes around the middle part and then through the hottest part, while the hydrocarbon gas passes through the middle part.
- the hydrocarbon gas is heated up to a point below which methane or other hydrocarbons will deposit carbon, and the air is heated up nearly to the temperature of the waste gas entering the exchanger.
- the waste gases leaving the exchanger are available for combustion purposes either as they are or after further cooling and cleaning as desired.
- the reduced granules from the bottom of the reduction shaft are removed by a water cooled screw conveyer through a pipe cooled externally. By this means they are cooled to atmospheric temperature.
- the reduced granules from the shaft may be conveyed while still hot into an electric furnace where they will be melted into a product containing but little carbon.
- the air passes through the cold part I8 of the exchanger I0, through the by-pass II, then l5 through the hot part I9 and by the pipe Il and the hydrocarbon passes through the middle part 20 of the exchanger and by the pipe Il to the chamber I5, in which is generated the reducing gas. Where additional heat is required 20 in the generator, this is supplied through electrodes IB.
- the reducing gas passes through the pipe I I to the bustle pipe for the shaft.
- the catalyzer may be contained in a muille or oven 25 or a series of the same and the heat applied externally by passing a flame or heating gases through fiues surrounding the muilles or ovens.
- the catalyzer may be contained in two or more stoves, which are alternately heated by 80 the passage of heating gases and utilized for the passage and heating of the mixture oi' hydrocarbon and air.
- the method of reducing iron ore or the like which consists in passing the ore through a kiln and then into and through a shaft, generating a gas comprising hydrogen and carbon monoxide by passing a hydrocarbon and air through a catalyzer and heating the same to a tempera- 40 ture above about 1500 degrees Fahrenheit, heat being supplied by the passage of a current of electricity through the catalyzer, and passing said gas rst through the charge in the shaft to accomplish the nal reduction and thence 5 through the kiln to accomplish a preliminary reduction.
- the method of reducing iron ore or the like which consists in passing the ore through a kiln and then into and through a shaft, gener- 50 ating a gas comprising hydrogen and carbon monoxide by passing a hydrocarbon and air through a catalyzer and heating the same to a temperature above about 1500 degrees Fahrenheit, heat being supplied externally, and passing u said gas rst through the charge in the shaft to accomplish the final reduction and thence through the kiln to accomplish a preliminary reduction.
Description
DeC- 3 1935- w. D. BROWN PRODUCTION OF SPONGE IRON original Filed June 5, 195.3
Ressued Dec. 3, 193.5 y
UNITED STATES PATENT OFFICE Serlll No. 674,430, June 5, 1933.
Application for reime June l'l, 1935, Serlll No. 27,122
3 Claim. (CL l5-14) If it is attempted to reduce iron oxide by hydrocarbons, I have found that deposition of carbon occurs and the resultant product is very much contaminated with carbon. The present 5 invention utilizes hydrocarbons in the reduction of iron ores and similar iron-bearing materials without such contamination, producing iron in the form of a spongy or granular product.
For this purpose the hydrocarbons are rst converted to a reducing gas consisting of a mixture of hydrogen and carbon monoxide. The conversion is accomplished by passing the hydrocarbon, such as natural gas, with a certain quantity of air through a catalytic chamber. 'Ihis chamber is filled with particles of firebrick, coke or graphite or a mixture of one or more, some of which have been dipped in a solution of nickel nitrate, dried and ignited. I have found that the quantityof air should be such that the oxygen contained therein is Just suiilcient to combine with the carbon of the hydrocarbon to form carbon monoxide, liberating the hydrogen.
The reaction of conversion of hydrocarbons with air to carbon monoxide and hydrogen is exothermic, but some hydrocarbons. such as natural gas do not produce sufficient heat to raise thegas to the high temperature desired (2000 FJ; consequently it is necessary to sup ply heat to the reaction. This heat may be supplied in various ways; as, for example, by passing an electric current through the catalyzer, or heat may be transferred through oven walls, or heat may be supplied by using intermittently two or more stoves in the usual manner.
By the term hydrocarbon is meant compounds of carbon and hydrogen. In this process I describe the use of natural gas, which is a mixture of methane, ethane, and higher members of the series such as propane. I do not desire to limit the invention to the use of natural gas, any volatile hydrocarbon such as mineral oil or benzol may be used. In the case of the hydrocarbons containing a high percentage of carbon it may not be necessary to heat the generator.
. I have also found that coke oven gas containing a mixture of hydrogen, carbon oxides and hydrocarbons can be used in place of natural gas.
I have also found that the mixture of carbon monoxide, hydrogen and nitrogen from the air, containing possibly traces of carbon dioxide. water and methane reduces oxides of iron, the
product containing above 90 per cent of the iron in the metallic state with but littlecarbon deposited.
I have also vfound that dense magnetite (FeaOq) when roasted in the presence of oxygen, changes into a porous form of oxide of 5 iron (FezOa) which is easily reduced by the above reducing gases. Y
I have found that, while the particles of this oxide of iron (FezOa) tend to adhere together and also that the FeO resulting from partial 10 reduction tends to adhere, when FeO is reduced by the above gases to metallic iron the particles at 1650 F. do not adhere but fall freely.
A particular process embodying the invention is the following: A mixture of air and natural l5 gas is passed through a chamber containing a cataiyzer, consisting of pieces of coke or graphite which have been dipped in a solution of nickel nitrate, dried and ignited. A current of electricity is passed through the chamber, thus 20 supplying the heat required. Both the air and the natural gas have been heated (to 1500- 1000 respectively), by passing counter-current with the waste gas from reduction through heat exchangers. On accolmt of the preheat, the 25 heat required to be supplied by electricity is not excessive. v
The reduction gas so produced at 2000" F. is conveyed to the reducing chamber. While I do not desire to limit the iorm or design of the 30 reducing chamber or chambers, I describe the following as a practicable arrangement. Reduction is accomplished in two chambers. The large part of the reduction is accomplished in a kiln and the nal reduction is accomplished in 35 a shaft. The partially reduced material from the kiln empties into the shaft. 'I'he reducing gas enters near the bottom of the shaft and extends upwards, reducing all but trace of any iron oxide remaining. I'he gases then pass into the 40 kiln where the main part of the reduction occurs. The gas ilrst reduces the bulk oi' the FeO to Fe and then passing on reduces the FeaO: to FeO. i i
The gases which entered the reducing ham?1 45 ber at 2000 F. have become somewhat cooler, due to the endothermic nature of the reaction and to radiation loss, but not sufficiently so to stop the reaction. At the temperature which prevails when FeO is reduced to Fe, I have 50 found that approximately 30 per cent of the original carbon monoxide and hydrogen have been used. As the gas proceeds. more of it is used in reducing FezO: to FeO.
The gases left contain considerable carbon 55 monoxide and hydrogen. Some of the gas (about per cent) is bled for other uses as described, and the remaining gas is passed into the preheating kiln. It is necessary to have the incoming ore (FezOs) at about 1830. consequently air is added to the gas in the preheater, thus raising the temperature to the necessary point. At the same time, dense crystals of magnetite (FeaOi), if present, are broken up and porous FezOa is formed. 'I'his latter oxide is much more reducible than the hard dense magnetite. The gas which is bled, containing as it does both sensible heat (temperature 1600*' F.) and heat of combustion, may be used for other purposes, but half of it, or 40 per cent oi' the entire gas after reduction, may be used to heat the generator unless the generator is heated electrically.
In the process here described, the waste gases pass through a heat exchanger, counter-current to air. 'Ihis air is later used in the generator. This heat exchanger is so constructed that the cold air passes through the cold part of the exchanger then passes around the middle part and then through the hottest part, while the hydrocarbon gas passes through the middle part.
By this means the hydrocarbon gas is heated up to a point below which methane or other hydrocarbons will deposit carbon, and the air is heated up nearly to the temperature of the waste gas entering the exchanger. The waste gases leaving the exchanger are available for combustion purposes either as they are or after further cooling and cleaning as desired.
The reduced granules from the bottom of the reduction shaft are removed by a water cooled screw conveyer through a pipe cooled externally. By this means they are cooled to atmospheric temperature. The reduced granules from the shaft may be conveyed while still hot into an electric furnace where they will be melted into a product containing but little carbon.
While I have described the use of air in the generatorto convert hydrocarbons to carbon monoxide and hydrogen, it is apparent that commercial oxygen, steam or carbon dioxide may be used as substitutes for air. Also. some of the waste gases may be returned and the carbon dioxide and water contained therein be used in the conversion. 'Ihe amount of heat required in the case of all of these, except oxygen, is greatly in excess of that required in the proposed process.
The accompanying drawing is a diagrammatic illustration of a suitable arrangement of apparatus.
'Ihe ore passes first through an inclined rotating preheating kiln I, thence through a slmilar reducing kiln 2, thence through a shaft 3 in which the nal reduction is eil'ected. The kilns and shaft form a substantially airtight circuit. The product is taken off through a tube 4 by a screw conveyer 5.
'I'he reducing gas enters the lower part of the shaft by tuyres from a bustle pipe 6. After passing through the shaft and reducing kiln a b portion of the hot gas is taken oil? through a conduit 1. The remainder passes through the preheating kiln where it is mixed with air introduced through a pipe B to raise its temperature, passing out nally through the stack 9. l0 The hot gases from the conduit 1 pass in succession through heat exchanger I0 to the discharge pipe I2.
The air passes through the cold part I8 of the exchanger I0, through the by-pass II, then l5 through the hot part I9 and by the pipe Il and the hydrocarbon passes through the middle part 20 of the exchanger and by the pipe Il to the chamber I5, in which is generated the reducing gas. Where additional heat is required 20 in the generator, this is supplied through electrodes IB. The reducing gas passes through the pipe I I to the bustle pipe for the shaft.
Instead of heating the catalyzer by an electric current, it may be contained in a muille or oven 25 or a series of the same and the heat applied externally by passing a flame or heating gases through fiues surrounding the muilles or ovens. Or the catalyzer may be contained in two or more stoves, which are alternately heated by 80 the passage of heating gases and utilized for the passage and heating of the mixture oi' hydrocarbon and air.
I claim:
1. The method of reducing iron ore or the like which consists in passing the ore through a kiln and then into and through a shaft, generating a gas comprising hydrogen and carbon monoxide by passing a hydrocarbon and air through a catalyzer and heating the same to a tempera- 40 ture above about 1500 degrees Fahrenheit, heat being supplied by the passage of a current of electricity through the catalyzer, and passing said gas rst through the charge in the shaft to accomplish the nal reduction and thence 5 through the kiln to accomplish a preliminary reduction.
2. The method of reducing iron ore or the like which consists in passing the ore through a kiln and then into and through a shaft, gener- 50 ating a gas comprising hydrogen and carbon monoxide by passing a hydrocarbon and air through a catalyzer and heating the same to a temperature above about 1500 degrees Fahrenheit, heat being supplied externally, and passing u said gas rst through the charge in the shaft to accomplish the final reduction and thence through the kiln to accomplish a preliminary reduction.
3. The process of claim 2, using coke-oven gas n as the hydrocarbon.
WILLIAM DARKE BROWN.
Publications (1)
| Publication Number | Publication Date |
|---|---|
| USRE19770E true USRE19770E (en) | 1935-12-03 |
Family
ID=2084158
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US19770D Expired USRE19770E (en) | Production of sponge ibxn |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | USRE19770E (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2417949A (en) * | 1943-08-21 | 1947-03-25 | Riveroll Elfego | Process for recovery of iron from ore |
| US2481217A (en) * | 1947-06-03 | 1949-09-06 | Standard Oil Dev Co | Process for a two-stage gaseous reduction of iron ore |
| US2752234A (en) * | 1955-07-07 | 1956-06-26 | United States Steel Corp | Process for continuous gaseous reduction of iron ore in a fluidized bed system |
| US2848316A (en) * | 1956-06-07 | 1958-08-19 | United States Steel Corp | Process for gaseous reduction of iron ore |
| US3072474A (en) * | 1961-03-21 | 1963-01-08 | Phillips Petroleum Co | Cokeless smelting of ore |
| US3136625A (en) * | 1961-08-22 | 1964-06-09 | Pullman Inc | Method for reducing metal oxides |
| US3136623A (en) * | 1960-11-04 | 1964-06-09 | Pullman Inc | Method for reducing metal oxides |
-
0
- US US19770D patent/USRE19770E/en not_active Expired
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2417949A (en) * | 1943-08-21 | 1947-03-25 | Riveroll Elfego | Process for recovery of iron from ore |
| US2481217A (en) * | 1947-06-03 | 1949-09-06 | Standard Oil Dev Co | Process for a two-stage gaseous reduction of iron ore |
| US2752234A (en) * | 1955-07-07 | 1956-06-26 | United States Steel Corp | Process for continuous gaseous reduction of iron ore in a fluidized bed system |
| US2848316A (en) * | 1956-06-07 | 1958-08-19 | United States Steel Corp | Process for gaseous reduction of iron ore |
| US3136623A (en) * | 1960-11-04 | 1964-06-09 | Pullman Inc | Method for reducing metal oxides |
| US3072474A (en) * | 1961-03-21 | 1963-01-08 | Phillips Petroleum Co | Cokeless smelting of ore |
| US3136625A (en) * | 1961-08-22 | 1964-06-09 | Pullman Inc | Method for reducing metal oxides |
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