US3865574A - Process for the production of low-sulfur prereduced iron pellets - Google Patents

Process for the production of low-sulfur prereduced iron pellets Download PDF

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US3865574A
US3865574A US273522A US27352272A US3865574A US 3865574 A US3865574 A US 3865574A US 273522 A US273522 A US 273522A US 27352272 A US27352272 A US 27352272A US 3865574 A US3865574 A US 3865574A
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pellets
temperature
iron oxide
carbon
sulfur
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US273522A
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English (en)
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Raymond H Long
William V Bauer
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CB&I Technology Inc
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Lummus Co
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Priority to US273522A priority Critical patent/US3865574A/en
Priority to AU58210/73A priority patent/AU484114B2/en
Priority to DE2336496A priority patent/DE2336496C2/de
Priority to JP8040973A priority patent/JPS5529132B2/ja
Priority to IT26800/73A priority patent/IT991294B/it
Priority to BE133681A priority patent/BE802581A/xx
Priority to GB3435873A priority patent/GB1444183A/en
Priority to SE7310086A priority patent/SE403137B/xx
Priority to CA176,814A priority patent/CA988722A/en
Priority to BR5466/73A priority patent/BR7305466D0/pt
Priority to ZA734932A priority patent/ZA734932B/xx
Priority to FR7326784A priority patent/FR2193879B1/fr
Priority to LU68061A priority patent/LU68061A1/xx
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Publication of US3865574A publication Critical patent/US3865574A/en
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    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0046—Making spongy iron or liquid steel, by direct processes making metallised agglomerates or iron oxide
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/24—Binding; Briquetting ; Granulating
    • C22B1/2406—Binding; Briquetting ; Granulating pelletizing
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present Invention discloses a process for produc- NY mg iron oxide pellets of low residual sulfur. in the pelletizing of finely divided ore with carbonaceous mate- [73] Asslgnee: The Lummus Company Bloomfield rials as binder, varying amounts of sulfur are intro prised. Green pellets are heated under conditions 22 Filed; Ju
  • the M960 Haworsonm H 75/3 pellets are further reduced with a stoichiometric 3,093,474 6/l963 Collin 75/3 X excess of reductant external to the pellet, with fast 3,2l8,l52 ll/l965 Sasabe 75/3 X heating to reduction temperature.
  • Residual Oil Preheat F "1 I Carbonize l 1 l l Pelletl ze Carbonlze l l Coking l l i Hydrocarbon 1 Low Recovery Reduction Carbon i i Lirriestane I High Reduction Screen M t 5.32m.
  • the mixture is fed to a pelletizer maintained at a lower temperature, where additional residual oil at a high temperature is sprayed thereon, with little or no cracking taking place, and pellets are formed in the A to 2 inch size range.
  • the pellets are passed to a coker maintained at a temperature of 900-l ,400 F. where the volatile content of the pellets is cracked and driven off. Since the amount of volatile material in the pellets is sufficiently low, vapor evolution during coking does not cause significant size degradation, but pellets of a distinct, finely porous structure are produced.
  • Such pellets are described in U.S. Pat. No. 3,420,656, also assigned to the same assignee as the instant application.
  • the coked pellets contain sufficient carbon to achieve the desired degree of reduction of iron oxides in the pellet.
  • the hot coked pellets are then passed to a calciner maintained at a temperature of about 1,800-2,300F. to form highly prereduced pellets. After reduction, the reduced pellets are screened and cooled. Cracked gas is recovered from the carbonizer and the coker and supplied to a combination still, from which by-products are recovered.
  • Partially reduced pellets of the above-described type are most useful as a blast furnace feed, and can be used as a portion of the ore burden or all of it.
  • the blast furnace is a very efficient reducing device, and does not require, or benefit from, using a very highly reduced burden (see, on this point, Agarwal and Pratt, The Thermodynamic Aspects of Using Partially Reduced Burdens," Transactions, AIME Ironmaking Conference, 1965).
  • liquid carbonaceous feedstocks contain varying amounts of sulfur, some of which will be found in the prereduced pellet. This will render such pellets less desirable for blast furnace use and, in many instances, unfit for electric furnace melting.
  • the general object of the present invention is to provide a process for producing prereduced pellets wherein residual sulfur in the prereduced pellets is diminished.
  • a further object of the invention is to provide prereduced pellets adapted for blast furnace use, and containing less than about 0.25 percent residual sulfur.
  • FIG. I is a simplified flow sheet illustrating a preferred embodiment of the invention adapted to produce highly prereduced pellets employing high-sulfur petroleum residual oils;
  • FIG. 2 is a chart chowing heating and reduction curves for conventional pellets and pellets made in accordance with the invention.
  • FIG. 3 is a simplified flow sheet illustrating an alternative embodiment of the invention.
  • the present invention achieves lowered sulfur levels by a controlled calcining treatment. It has been determined that pellets of less than percent prereduction should be heated quickly to a calcining temperature in the range of l,800-2,500F., generally l,900-2,l00F. to maximize desulfurization. Pellets that will be highly prereduced, on the other hand, contain more carbon and profit from a slow heating to the calcining temperature. However, high prereduction and fast heating can be combined by limiting the carbon in the pellet, and completing the reduction with external carbon. Desulfurization is aided by the addition of known sulfur scavenging compounds.
  • Pellets containing residual sulfur to be treated in accordance with this invention maybe prepared in a variety of ways.
  • the carbonizer may be a rotatingdrum equipped with means for injecting hot residual oil, to
  • seed pellets which are then grown to desired size.
  • Recycled coke fines, ore fines etc. may be used as seed particles.
  • coke from resid produced in a delayed coker and then comminuted may be employed.
  • the carbonizer product is used externally to the ore pellets in the high reduction stage, and no sulfur scavenger is added in the car bonizer.
  • the oil For pelletizing, it is preferable to deliver the oil at a temperature where it flows readily but below its cracking temperature. With many residual oils, a temperature in the range of 300-750F is satisfactory.
  • the finely divided ore is heated in a carbonizer to a much higher temperature, 900l ,300F. The resultant average temperature is usually in the 750-l,l00F range.
  • a sulfur scavenging compound may be first sprayed on the hot ore inappropriate amount, when desired. The sulfur-containing oil is then sprayed onto the agitated ore and cracks immediately on contact therewith. Since the carbon is layed down on the ore particles, the particles will grow in size even though little if any agglomeration takes place.
  • Feed to the pelletizer is preferably 50-80 percent minus 325 mesh. It is desireable to limit oil injection into the pelletizer to that level which leads to optimum pelletizer operation and best green pellet properties, usually 7 to 50wt. percent of the solids feed.
  • Pelletizing is carried out with the ore-carbon mixture and the residual oil at a temperature of 350-800F. (preferably 400-750F.) though variations may occur with particular oils. Desired pellet size is usually in the A to 2 inch range, depending on end use. Any of the well-known types of pelletizers that can operate at elevated temperatures can be employed in this step. The total amount of carbon of any form incorporated into the pellet depends on reduction desired and end use, as will hereafter become apparent.
  • the green pellets are conveyed while hot directly to the coking kiln.
  • the kiln must be heated by means other than direct firing so as to permit recovery of gases resulting from cracking of the hydrocarbon binder.
  • the temperature of the pellets is raised to about 900-l,400, preferably l,00O-l ,300F., and hard, strong pellets are produced having a porous finegrained coke structure.
  • the total amount of residual oil used in the carbonization and pelletizing steps is controlled so that the carbon content of the pellets is slightly greater than the stoichiometric quantity required for the desired degree of total reduction.
  • the reduced pellets are cooled to a temperature below 250F. in a protected, non-oxidizin g atmosphere.
  • p'ellet preparation may be carried out in the manner described in the above mentioned U.S. Patents for some of the processing schemes herein disclosed.
  • an intimate ore-carbon mixture may be prepared by mixing any low-volatile carbonaceous material with the ore. Finely ground coal, preferably deashed, or coke may be used in this service. Fluxes and sulfur-acceptors or substances conducive to sulfur elimination should be added to the ore-carbon mixture.
  • the amount of carbon present and in contact with the pellet in the reduction kiln determines the degree of prereduction that will be achieved. In accordance with the present invention, this can be broken down into five categories or schemes. which are summarized hereinbelow in Table l.
  • the first scheme relates toproducing blast furnace pellets of low prereduction, preferably 35-50 percent. Carbon for reduction is provided solely by the liquid binder material, without added carbon. The binder-to-solids ratio is chosen to provide good pelletizing operation and high pellet strength. Depending on the binder or, more accurately, its Conradson Carbon number, sufficient integral carbon will be laid down in the pellet for the desired reduction. Generally residual oils will provide enough carbon for 25-60 percent reduction.
  • the third scheme differs from the second in that enough solid carbon is added to make high prereduction percent) possible. in this instance, heating to the calcining temperature should be slow, to achieve desired desulfurization.
  • the fourth scheme can be visualized as combining the first or second schemes (i.e., relatively low reduction with fast heating) and a second reduction treatment including added carbon external to the pellets.
  • the last scheme utilizes a highly carbonaceous internal binder, such as coal tar pitch, with fast heating for reduction of up to 85 percent, and slow heating where even greater reduction is desired.
  • a highly carbonaceous internal binder such as coal tar pitch
  • FIG. 1 illustrates, in greatly simplified form, the fourth scheme for producing highly reduced pellets (as much as percent).
  • the pellets In forming the pellets, only sufficient residual oil is used so that carbon remaining after coking will be consumed in reducing the pellet about 25-50 percent.
  • the first reduction is carried out with fast heating to reduction temperature in a direct fired furnace, such as a rotary kiln. Essentially all of the carbon in the pellet is consumed in this reduction, and the resulting partially reduced pellets are quite porous. They are immediately charged to the high reduction kiln, along with a substantial stoichiometric excess of carbon and limestone or other sulfur scavenger, the particle size of these additives after reduction is complete being sufficiently smaller than the pellets to permit subsequent separation by screening. For example, if the pellets are in the to A-inch range, the reductant should pass a %-inch screen.
  • the high reduction kiln is also directly tired, and it is preferred that the load factor be kept low, about 8 to 15 percent, preferably below 12 percent, to maximize heat transfer from the kiln walls to the bed and by direct radiation from the flame. Because of the pellet porosity, reduction proceeds much faster than with solid pellets (i.e., CO can penetrate into the pellet and CO can leave much quicker).
  • the excess carbon for the high reduction stage may optionally be carbonized residual oil, as shown on the drawing, agglomerated to a proper size, or an external source of carbon may be used, including coal or coke from any source, crushed to the desired size range.
  • the burden leaving the high reducer kiln is subjected to splitting operations. [f the size of carbon pellets is carefully controlled as previously taught, it is convenient to use screening to achieve the desired splits.
  • the burden is first passed over a screen to retain and discharge finished pellets.
  • the underflow is again subjected to separation according to size.
  • the retained second cut consists primarily of partially used coke which is conveyed back to the feed end of the high reducer for recycle.
  • the undersize material consists of some coke fines, calcium compounds and gangue "and ferruginous fines. Depending upon local and economic factors, this stream may be cooled and discarded or subjected to magnetic separation or other treatment for recovery of iron and carbon values.
  • Prereduction using external carbon is not in itself novel; the well-known SL-RN process utilizes this approach.
  • the rate of reduction is relatively slow, and it is apparently difficult to achieve high levels of pre-reduction. Residence times of many hours are required and high operating temperatures, sometimes over 2,000F. create attendant fusion and ringing problems.
  • a high load factor (20-40 percent), large kilns and a long residence time are all necessary to achieve reasonable production, because of poor reactivity and the great excess of carbon present.
  • FIG. 2 shows heating and reduction curves for pellets of the invention and conventional pellets (purchased):
  • Comparable reduction levels are attainable in a fraction of the residence time required by conventional pellets.
  • the gas make has a significantly lower CO/CO ratio. At comparable levels of prereduction, the ratio would be even more favorable. This implies more efficient utilization of reductant as well as significant reduction in heat duty and equipment size.
  • the high reactivity of the pellets permits reduced temperatures during the terminal phase of reduction (from about 40 to 60 percent reduction to the desired product pellet reduction level), a range particularly susceptible to tackiness and kiln ranging problems.
  • the cooling pellets may be tumbled with finely divided ore or limestone, both of which will tend to fill the pores (and both of which will be preheated), with the same effect of increasing resistance to weathering.
  • schemes 1, II, N, and VA require fast heating for proper desulfurization.
  • Effective desulfurization is achieved by heating the pellets rapidly, in a period under 1 hour and preferably under 45 minutes, from a temperature of 1,500F. to an upper temperature of l,800-2,500F., preferably 1,9- O0-2,l00F., and maintaining such upper temperature for a period of 15 minutes to 6 hours, and preferably 30 minutes to 2 hours.
  • Desulfurization is defined as:
  • additives may consist of metal chlorides, preferably alkali or alkaline-earth chlorides, or FeCl alone or in combination with calcium sulfate, alkalineearth oxides or carbonates.
  • the additives may be incorporated in the pellets by feeding with the ore to the pelletizer and to the carbonizer, or by suspension in finely divided form in the binder prior to spraying into the pelletizer or the carbonizer.
  • Water soluble additives viz., the metal chlorides
  • the additives be uniformly dispersed in the pellet, the particle size of the dispersed additives being at least under 100 mesh and preferably 100 percent under 200 mesh.
  • the dosage of additives may be quite low; good results have been achieved with dosages in the range of 0.01 to percent, but for consistent results in the range of 0.5 to 3 percent is preferred. These dosages are expressed in terms of weight percent relative to ore used.
  • pellets and fines generated in the process are ground to about 80 percent minus 325 mesh size.
  • the carbonizer product solids are comminuted to about the same size range.
  • the mixture at this stage is passed to the pelletizing drum with preheated ore, where additional quantities of the pre heated oil are sprayed on and pellets are formed.
  • the pellets contain 7.6 percent solid carbon and 13.2 percent residum.
  • the hot pellets which are mostly in the to inch size range, are conveyed to the coker.
  • a circulating load of hot sand may be employed.
  • the coker discharge is screened and the sand is recirculated.
  • Run A demonstrates the advantage of slow heating for high prereduction, and shows that a high final temperature is unnecessary.
  • Run B shows that for lower prereduction fast heating is preferable.
  • Run C for 85 percent reduction, indicates that fast heating is preferable, but this is a gray area.
  • the oil is preheated to 600F. before spraying, and 60 ing reduction, without any desulfurization, an increase in reported sulfur content would be expected, and decreases in sulfur content are proportionally greater than the numbers indicate.
  • the product pellets were uniform, dense, and free of fissures or defects.
  • the conventional pellets yielded product pellets of varying diameters (corresponding generally to variations in degree of reduction), and showed considerable cracks and some fragmentation.
  • pelletizing said ore and a minor proportion of'a sulfur-scavenging compound by spraying said carbonaceo us material thereon while agitating same, said carbonaceous material being heated to a flowable temperature and maintaining the temperatures in the pelletizing mixture below the cracking temperature and said carbonaceous material;
  • a process for producing prereduced iron oxide pellets of low-sulfur content from ore and a sulfurbearing fluid carbonaceous material comprising:
  • pelletizing said mixture by spraying said carbonaceous material thereon while agitating same, said carbonaceous material beig heated to a flowable temperature and maintaining the temperature in the pelletizing mixture below the cracking temperature of said carbonaceous material;
  • a process for producing highly prereduced iron oxide pellets of low-sulfur content from ore and a sulfur-bearing fluid carbonaceous material comprising:
  • pelletizing said ore mixture by spraying said carbonaceous material thereon while agitating same, said carbonaceous material being heated to a flowable temperature and maintaining the temperature in the pelletizing mixture below the cracking temperature of said carbonaceous material;
  • a process for producing highly procedured iron oxide pellets of low-sulfur content from ore and a sulfur-bearing fluid carbonaceous material comprising:
  • pelletizing said ore and a minor proportion of a sulfur-scavenging compound by spraying said carbonaceous material thereon while agitating same, said carbonaceous material being heated to a flowable temperature and mantaining the temperature in the pelletizin g mixture below the cracking temperature of said carbonaceous material;
  • a process for producing prereduced iron oxide pellets of low-sulfur content from iron oxide pellets containing integral carbon comprising:
  • the iron oxide pellets subjecting the iron oxide pellets to coking conditions to coke said binder and produce integral carbon, said binder providing at least a portion of the integral carbon in said pellets, the coked pellets containing sufficient integral carbon to effect from about 25 to about percent prereduction of the iron oxide pellets; heating the iron oxide pellets containing integral carbon to raise the temperature of the iron oxide pellets to a final prereduction temperature of from about l,800 F, during said heating the temperature of the pellets being raised from a temperature of about 1,500F to the final reduction temperature in a time of less than about 1 hour; and
  • sulfur scavenging compound is at least one member selected from the group consisting of calcium chloride, magnesium chloride, ferric chloride, a mixture of sodium chloride and calcium carbonate and a mixture of sodium chloride and calcium oxide.
  • a process for producing prereduced iron oxide pellets of low-sulfur content from iron oxide pellets containing integral carbon comprising:
  • iron oxide pellets subjecting the iron oxide pellets to coking conditions to coke said binder and produce integral carbon, said binder providing at least a portion of the integral carbon in said pellets, the coked pellets containing sufficient carbon to effect a greater than 85 percent prereduction; heating the iron oxide pellets containing integral car bon to raise the temperature of the iron oxide pellets to a final reduction temperature of from about l,800 to about 2,500F, during said heating the temperature of the pellets being raised from a temperature of l,500F to the final reduction temperature in a time of from 1 to 6 hours; and
  • the sulfur scavenging compound is at least one member selected from 5 the group consisting of calcium chloride, magnesium chloride, ferric chloride, a mixture of sodium chloride and calcium carbonate and a mixture of sodium chloride and calcium oxide.
  • a process for producing 70-85 percent prereduced iron oxide pellets of low-sulfur content from ore and a coal tar pitch comprising:
  • pelletizing said ore and a minor proportion of a sulfur-scavenging compound by spraying said pitch thereon while agitating same, said pitch being heated to a flowable temperature and maintaining the temperature of the pelletizing mixture below the cracking temperature of said pitch;
  • the coked pellets conbeing raised from a temperature of 1,500F to the taining sufficient integral carbon to effect a greater .final reduction temperature in a time of from 1 to than 85 percent prereduction; -6 hours; and heating the iron oxide pellets containing integral carholding the iron oxide pellets at the'final reduction bon to raise the temperature of the pellets to a final temperature to produce prereduced iron oxide pelreduction temperature of from 1,900 to 2,l0OF, lets.

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US273522A 1972-07-20 1972-07-20 Process for the production of low-sulfur prereduced iron pellets Expired - Lifetime US3865574A (en)

Priority Applications (13)

Application Number Priority Date Filing Date Title
US273522A US3865574A (en) 1972-07-20 1972-07-20 Process for the production of low-sulfur prereduced iron pellets
DE2336496A DE2336496C2 (de) 1972-07-20 1973-07-18 Verfahren zur Herstellung vorreduzierter Eisenoxid-Pellets mit niedrigem Schwefelgehalt
JP8040973A JPS5529132B2 (US20110009641A1-20110113-C00116.png) 1972-07-20 1973-07-18
AU58210/73A AU484114B2 (en) 1972-07-20 1973-07-18 Process for the production of low sulfur prereduced iron pellets'
BE133681A BE802581A (fr) 1972-07-20 1973-07-19 Procede pour produire des pastilles d'oxyde de fer hautement reduites a faible teneur en soufre
GB3435873A GB1444183A (en) 1972-07-20 1973-07-19 Process for the production of low-sulphur prereduced iron pellet
IT26800/73A IT991294B (it) 1972-07-20 1973-07-19 Procedimento per la produzione di perle di ferro preridotto a basso contenuto in zolfo
SE7310086A SE403137B (sv) 1972-07-20 1973-07-19 Forfarande for framstellning av forreducerade jernoxidkulor med lag svavelhalt
CA176,814A CA988722A (en) 1972-07-20 1973-07-19 Process for the production of low-sulfur prereduced iron pellets
BR5466/73A BR7305466D0 (pt) 1972-07-20 1973-07-19 Processo para a producao de peletas de ferro pre-reduzidas de baixo teor de enxofre
ZA734932A ZA734932B (en) 1972-07-20 1973-07-19 Process for the production of low-sulfur prereduced iron pellets
FR7326784A FR2193879B1 (US20110009641A1-20110113-C00116.png) 1972-07-20 1973-07-20
LU68061A LU68061A1 (US20110009641A1-20110113-C00116.png) 1972-07-20 1973-07-20

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US (1) US3865574A (US20110009641A1-20110113-C00116.png)
JP (1) JPS5529132B2 (US20110009641A1-20110113-C00116.png)
BE (1) BE802581A (US20110009641A1-20110113-C00116.png)
BR (1) BR7305466D0 (US20110009641A1-20110113-C00116.png)
CA (1) CA988722A (US20110009641A1-20110113-C00116.png)
DE (1) DE2336496C2 (US20110009641A1-20110113-C00116.png)
FR (1) FR2193879B1 (US20110009641A1-20110113-C00116.png)
GB (1) GB1444183A (US20110009641A1-20110113-C00116.png)
IT (1) IT991294B (US20110009641A1-20110113-C00116.png)
LU (1) LU68061A1 (US20110009641A1-20110113-C00116.png)
SE (1) SE403137B (US20110009641A1-20110113-C00116.png)
ZA (1) ZA734932B (US20110009641A1-20110113-C00116.png)

Cited By (13)

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US4971622A (en) * 1988-01-05 1990-11-20 Middelburg Steel And Alloys (Proprietary) Limited Sulphur and silicon control in ferrochromium production
US5213742A (en) * 1990-09-11 1993-05-25 Vitaphore Corporation Method of producing pores of controlled geometry on a thermoplastic polymer
BE1010766A3 (fr) * 1996-11-25 1999-01-05 Centre Rech Metallurgique Procede pour fabriquer une eponge de fer a faible teneur en soufre.
US6036744A (en) * 1996-03-15 2000-03-14 Kabushiki Kaisha Kobe Seiko Sho Method and apparatus for making metallic iron
US6342089B1 (en) * 1997-09-02 2002-01-29 Mcgaa John R. Direct reduced iron pellets
US20050028643A1 (en) * 2002-10-08 2005-02-10 Hidetoshi Tanaka Method for producing titanium oxide containing slag
EP1929051A2 (en) * 2005-08-30 2008-06-11 E.I.Du pont de nemours and company Ore reduction process and titanium oxide and iron metallization product
US20100237280A1 (en) * 2007-10-15 2010-09-23 John James Barnes Ore reduction process using carbon based materials having a low sulfur content and titanium oxide and iron metallization product therefrom
US20100329935A1 (en) * 2009-06-25 2010-12-30 Mcgehee James F Apparatus for Separating Pitch from Slurry Hydrocracked Vacuum Gas Oil
US20100326887A1 (en) * 2009-06-25 2010-12-30 Mcgehee James F Process for Separating Pitch from Slurry Hydrocracked Vacuum Gas Oil
AU2012200914B2 (en) * 2005-08-30 2012-05-03 E. I. Du Pont De Nemours And Company Ore reduction process and titanium oxide and iron metallization product
US8231775B2 (en) 2009-06-25 2012-07-31 Uop Llc Pitch composition
US9150470B2 (en) 2012-02-02 2015-10-06 Uop Llc Process for contacting one or more contaminated hydrocarbons

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US3219436A (en) * 1962-06-30 1965-11-23 Metallgesellschaft Ag Method for reducing iron oxides into sponge iron
US3314780A (en) * 1964-07-07 1967-04-18 Inland Steel Co Process of pelletizing ore
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US2811434A (en) * 1954-12-21 1957-10-29 Nat Lead Co Process for treating ilmenite-containing materials to produce metallic iron concentrates and titanium dioxide concentrates
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US3427148A (en) * 1966-10-10 1969-02-11 Bergwerksverband Gmbh Process of producing iron-coke bodies
US3495971A (en) * 1967-05-19 1970-02-17 Mcdowell Wellman Eng Co Smelting furnace charge composition and method of making same
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US4971622A (en) * 1988-01-05 1990-11-20 Middelburg Steel And Alloys (Proprietary) Limited Sulphur and silicon control in ferrochromium production
US5213742A (en) * 1990-09-11 1993-05-25 Vitaphore Corporation Method of producing pores of controlled geometry on a thermoplastic polymer
US5332626A (en) * 1990-09-11 1994-07-26 Vitaphore Corporation Pores of controlled geometry on a thermoplastic polymer
US6036744A (en) * 1996-03-15 2000-03-14 Kabushiki Kaisha Kobe Seiko Sho Method and apparatus for making metallic iron
BE1010766A3 (fr) * 1996-11-25 1999-01-05 Centre Rech Metallurgique Procede pour fabriquer une eponge de fer a faible teneur en soufre.
US6342089B1 (en) * 1997-09-02 2002-01-29 Mcgaa John R. Direct reduced iron pellets
US20050028643A1 (en) * 2002-10-08 2005-02-10 Hidetoshi Tanaka Method for producing titanium oxide containing slag
US20080069763A1 (en) * 2002-10-08 2008-03-20 Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd) Method for manufacturing titanium oxide-containing slag
US8088195B2 (en) 2002-10-08 2012-01-03 Kobe Steel Ltd. Method for manufacturing titanium oxide-containing slag
US20090217784A1 (en) * 2005-08-30 2009-09-03 E.I. Du Pont De Nemours And Company Ore reduction process and titanium oxide and iron metallization product
EP1929051A2 (en) * 2005-08-30 2008-06-11 E.I.Du pont de nemours and company Ore reduction process and titanium oxide and iron metallization product
US7780756B2 (en) 2005-08-30 2010-08-24 E.I. Du Pont De Nemours And Company Ore reduction process and titanium oxide and iron metallization product
AU2012200914B2 (en) * 2005-08-30 2012-05-03 E. I. Du Pont De Nemours And Company Ore reduction process and titanium oxide and iron metallization product
US20100285326A1 (en) * 2005-08-30 2010-11-11 E. I. Du Pont De Nemours And Company Ore reduction process and titanium oxide and iron metallization product
EP1929051A4 (en) * 2005-08-30 2008-10-15 Du Pont RESTRICTED METHOD AND TITANIUM OXIDE AND IRON METALLIZATION PRODUCT
US20100237280A1 (en) * 2007-10-15 2010-09-23 John James Barnes Ore reduction process using carbon based materials having a low sulfur content and titanium oxide and iron metallization product therefrom
US8372179B2 (en) 2007-10-15 2013-02-12 E I Du Pont De Nemours And Company Ore reduction process using carbon based materials having a low sulfur content and titanium oxide and iron metallization product therefrom
US20100326887A1 (en) * 2009-06-25 2010-12-30 Mcgehee James F Process for Separating Pitch from Slurry Hydrocracked Vacuum Gas Oil
US20100329935A1 (en) * 2009-06-25 2010-12-30 Mcgehee James F Apparatus for Separating Pitch from Slurry Hydrocracked Vacuum Gas Oil
US8202480B2 (en) 2009-06-25 2012-06-19 Uop Llc Apparatus for separating pitch from slurry hydrocracked vacuum gas oil
US8231775B2 (en) 2009-06-25 2012-07-31 Uop Llc Pitch composition
US8540870B2 (en) 2009-06-25 2013-09-24 Uop Llc Process for separating pitch from slurry hydrocracked vacuum gas oil
US9150470B2 (en) 2012-02-02 2015-10-06 Uop Llc Process for contacting one or more contaminated hydrocarbons

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LU68061A1 (US20110009641A1-20110113-C00116.png) 1973-09-26
DE2336496A1 (de) 1974-01-31
GB1444183A (en) 1976-07-28
JPS5529132B2 (US20110009641A1-20110113-C00116.png) 1980-08-01
JPS4944924A (US20110009641A1-20110113-C00116.png) 1974-04-27
BR7305466D0 (pt) 1974-08-15
ZA734932B (en) 1974-06-26
FR2193879A1 (US20110009641A1-20110113-C00116.png) 1974-02-22
AU5821073A (en) 1975-01-23
IT991294B (it) 1975-07-30
DE2336496C2 (de) 1982-06-24
CA988722A (en) 1976-05-11
SE403137B (sv) 1978-07-31
BE802581A (fr) 1973-11-16
FR2193879B1 (US20110009641A1-20110113-C00116.png) 1980-10-17

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