专利摘要:
A method for direct reduction of iron in a shaft reduction furnace. Spent gas from the furnace is upgraded in reductant by removal of CO2 and water to form an upgraded gas. A fossil fuel is gasified to produce a hot gas which is tempered with a first stream of upgraded gas. The mixture is desulfurized by reaction with lime to produce hot desulfurized gas. A second stream of upgraded gas is heated and mixed with the hot desulfurized gas to produce hot reducing gas.
公开号:SU1052165A3
申请号:SU792806953
申请日:1979-08-14
公开日:1983-10-30
发明作者:Чарльз Мейсснер Дейвид;Валтер Санзенбахер Чарльз
申请人:Мидрекс Корпорейшн (Фирма);
IPC主号:
专利说明:

2. A method according to claim 1, characterized in that a portion of the cold recycle gas is added before mixing with the preheated portion.
3. The method according to claim 1, from 1 to 5 and from the fact that part of the cold recycle gas is fed to the cooling zone of the reactor for gas desulfurization.
  one :.
This invention relates to the direct production of iron in a shaft furnace.
Most plants for direct recovery of reduced iron use natural gas as a source of reducing agent. Natural gas is reformed in order to obtain reducing agents GO and H2. ;.,.,; ,: . .
Installations are known that use coal as a source of reducing agent in rotary roasting processes, for example, the SL / RN process, according to coal, it is reduced directly to Mecte in a furnace without separate gasification of coal to produce CO and.
Rotary roasting processes. lack of efficiency associated with the use of coal; as two thirds are burned in; furnaces in order to provide heat and only one third; is used to obtain a stand-by dispersed gas for direct recovery. This leads to; A large amount of coal is required to get 5.0-6.0 Gcal per metric; tonnes of directly reduced iron, in contrast. in more efficient processes with natural gas at a rate of 3–3.5 gcal per ton of sponge iron. :. ..::; , u ...,
The closest to the proposed technical technical result and achievable result is the reduction of iron oxide in a shaft furnace with countercurrent top-loading material and a hot reducing gas consisting of a mixture of recycled and desulfurized gas from gasification of solid fuel with a quality indicator not lower than 6.5 C2.
However, the method is complicated and
not practical enough for industrial development, since the hot gas from the coal gasifier contains a low ratio of reducing agents (CO and H2) to oxidizers (vapors) and can be used effectively in direct reduction of iron.
The purpose of the invention is to reduce heat costs.
The goal is achieved by the fact that according to the method of reducing iron oxide, including the reduction of material loaded from the top and a hot reducing gas consisting of a mixture of recycled and desulfurized gas from gasification of solid fuel with a partial flow rate of not less than 6.5, part 1Р of circulating reducing gas is added to the gasification obtained at the outlet from the gasifier before the desulfurizer, and the rest of the heating section g to 60–900 e and mix the flow, from Desulfuratropa before transfer to the recovery zone ....;, .-,. .; . .
A portion of the cold recycle gas is added before mixing with the heated portion. ,
A portion of the cold recirculated gas is fed to the zone of the gas heater of the reactor for gas desulfurization.
The drawing shows a diagram of the implementation of the method.
 The diagram shows pech1 with a refractory coating of a mine type with protivotoksm material and reductant. Sub-material 2 (oxide in the form of Oxide Rocks and / or large ore with a nominal size of, within 530 mm is passed into the feed hopper 3 and the furnace through the nutrient line 4 to create a charge in the furnace. The removed iron pellets and / or lump product are drained from the furnace the lower aoHta furnace through the exhaust line 5 to the discharge conveyor 6, the speed of which controls the rate of descent of the charge through. 1. 1. ....
Fresh reducing reducing gas is introduced into the furnace 1 through the inlet line 7 for hot gas and gas inlets 8 located in the refractory wall in the middle zone of the furnace. The goy reducing gas flows inwards, then upwards, in countercurrent, in connection with the descending charge. Exhaust reducing gas (upper gas) containing CO; / exits through the charge in the upper part of the furnace at the level of the load formed by the angle of repose of iron oxide through the nutrient line 4 and leaves the furnace through the discharge line 9.,
The lower zone of the furnace 1 is circulated by a cooling gas to cool the reduced iron O before it is discharged from the furnace. The cooling furnace includes an inlet 10 / through which the gas enters the distribution gas cooling element 11 inside the furnace 1 / gas collection unit 12 for cooling gas, located 1 above the distribution elements in the furnace, output gas 13 for cooling gas and an external gas recirculation system having a scrubber cooler 14 and a recirculation blower 15.
The natural fuel gasifier 16 (using oxygen or oxygen and HVO / ko; gore) is injected through injector 17, used to gasify crushed fossil fuels, and coal, lignite or charcoal impregnators, in order to get the hot gas that escapes from the gasifier through conduit 19. The ash that remains after gasification of the fuel is removed from the gas stove through the emission of 20 ash.
The spinning gas coming out of the furnace through the exhaust line 9 (is cooled and cleaned of dust in the scrubber cooler 21, then enters the pipeline 22. A part of the cooled top gas is removed from the system through the drainage pipe 23 and is used as a fuel gas to produce steam. The second part of the cooled gas is removed through line 24 and is used as fuel for the burner. A third part of the cooled top gas is compressed by the gas compressor 25 and then injected through line 26 into a conventional regenerator The CO2 evacuation unit 27. In this unit, the main part of the CO2 is removed from the gas in order to obtain a gas enriched with a reducing agent, which is removed through conduit 28. A part of the gas enriched with a reducing agent is supplied to the mixing pipeline 29 for mixing with hot gas from gasification the torus in line 19 to a temperature below the solidification temperature of the ash. This mixing gas can be introduced alternately into the gas removal zone from the gasifier 16, where it will not adversely affect the gasification temperature; ..
The hot gasifier gas in line 19, after being mixed with gas from the mixing pipe 29, is partially cooled and introduced into gas desulphurizer 30 through gas inlet tube 31. Desulphurizer 30 is a shaft furnace with a refractory coating, in the upper part of which through a feed hopper and The feed tube 32 is introduced in the form of particles of limestone to form a charge in the desulfurizer.
Mixed hot gas from the gas inlet tube 31 is introduced into the desulfurizer through gas inlets 33 located in the refractory wall in the middle zone of the Furnace. Egot gas flows inward through the mixture with a countercurrent with respect to the descending mixture. The hot desulfurized gas is withdrawn from the tanks to the load level 34 and then through the outlet line 35. The lime that has been introduced to the reaction, sulfur containing sulfur and unreacted limestone residue is removed from the desulfurator via discharge pipe 36 to the discharge conveyor 37. Removal of the remaining particles after the reaction of the material to the discharge conveyor 37, the Cherez non-discharge conveyor 36 creates a gravitational flow and controls the speed of the charge passing through the gas 30 desulfurizer. A small amount of purified reducing gas, as a cooling gas for cooling the charge before it is unloaded, is fed through the pipe into the cooling gas distribution element 39, located in the lower desulfator zone 30. This coolant gas flows upwards, through the desulfator and is heated hot falling charge until the gas reaches the middle zone ..
Gas preheater 40 serves to heat a gas-enriched gas inlet coming from conduit 41 to a temperature that is necessary for use. it as a reducing gas in the reduction furnace 1. The preheater including the heating ones. the tubes 42, one or more burners 43 and the gas discharge pipe 44. The hot gases coming from the discharge pipe 44 are preferably used in a heat exchanger (not shown) to heat the hot air of the source 45 for the - burners 43 The fuel for the burner 43 is is the top gas introduced through conduit 24. The heated, enriched with reducing agent, exits gas preheater 40 through conduit 46, mixes with hot de-sulfurized gas, which comes from desulphurizer 30 and mixes with cold m enriched with a reducing gas flowing through the pipe 47, and acquires the temperature that must have a gas at the entrance to the furnace. This final gas mixture becomes a reducing reducing gas introduced into the reduction furnace 1 through the gas inlet line 7.
In the direct reduction of iron, a shaft-type reducing furnace with a counter-current ensures the highest thermal effect. efficiency in which the reducing gas and the ore are in a counter-current state, relative to each other. With this relative movement of gas and rock, the hot reducing gas serves not only to reduce iron oxide to metallic iron, but also to heat the iron oxide to its temperature of reduction.
The countercurrent kiln also has the highest chemical efficiency of all reduction furnaces of any type, provided that the hot reducing gas supplied to the furnace has a sufficiently high quality indicator, which is expressed as the ratio of reducing agents (CO- and H) to oxidants ( CO and.) In the gas mixture. Experience in the industrial use of natural gas installations has shown that in order to obtain the full chemical efficiency of a shaft reduction furnace with countercurrent, the quality indicator of the reducing gas must be at least eight.
When gasifying crushed solid fossil fuels, such as stone or lignite, in a partially-oxidized gasifier, such as gas preheater 40, produces a gas, predominantly containing CO, H, CO2 and% 0 ..
The invention is based on gasification of a typical subtuminous coal of coal using oxygen, H2O, and crushed coal in a layered type gasifier that produces hot gas containing mainly CO, HL, COg, and. The gasification temperature in such a gasifier is usually equal. At this temperature, the ash of the stone coal becomes liquid, is poured with water, and is removed from the bottom of the gasifier as slag.
An example. A hot reducing gas, whose quality index is 10, at a typical preferred temperature of 815s is introduced into the reduction furnace 1 through the gas inlet line 7, CO and H contained in the gas react with iron oxide, resulting in CO,
5 and metallic iron. In the reduction of iron oxide to metallic iron, only a fraction of the reducing agents (CO and H) are used, which can be reintroduced after removal of the oxidizing agents. This thermodynamic situation leads to the fact that the spent reducing gas leaving the furnace through the exhaust line 9 has a quality indicator of 1.5. In the gas scrubber cooler 21, a large amount of steam is condensed and removed from the gas, which results in the quality indicator of the cooled top gas
0 is 2. This gas is good fuel for combustion, but does not have a reducing potential for direct reduction of iron.
Part of the top gas with the indicator
5, a quality equal to 2 is used as fuel for the burner 43 of the gas preheater 40. Another part of the gas is removed from the system through the drain pipe 23 and is used as a fuel for heating the evaporator (not shown), which creates steam CO2 removal Most of the top gas is recycled through the CO2 removal unit 27, which leads to the enrichment of the gas withdrawn through the secondary pipeline 28. The reducing gas, whose quality indicator is high (23), is used in four directions.
The hot gas exiting the natural fuel gasifier 16 via line 19 has a temperature of 1370 ° C and a quality score of 6.5. The gas contains HgS and COS from sulfur in coal, some amount of charcoal unreacted in the reaction, and some drops of ash residue. In order to cause solidification of the liquid ash droplets in the hot gas and transfer. through pipelines, the flow in the mixing pipe 29 of the cold gas rich in reducing agent is mixed with hot gas so as to bring the temperature of the mixture to 950 ° C in the inlet tube 31 to the desulfurizer 30. This causes the quality indicator in the inlet tube 31 to become 9 ..
The desulphurizer 30 is supplied as lime particles. In order for the mixture to have good gas permeability, the particle size is preferably 3-20 mm. The mass flow rate of the hot gas introduced into the desulphurizer is very high relative to the speed of the cold limestone fed into the desulfurizer. This leads to the fact that the limestone very quickly acquires the temperature of the gas when it rises directly below level 34 in load. This results in very rapid calcification of the lime by obtaining calcined lime, which reacts with HgS and COS and removes these components from the gasified gas. Burnt lime may be supplied instead of limestone, but it is economically disadvantageous. The hot gasified gas is brought to the desulfurizer 30 before being fed to the desulfurator 30 by mixing with the cold, enriched with reducing agent. By reducing the oxidizer content in the hot gas by mixing it with high-quality gas, it is enriched with the reducing agent, which helps to remove sulfur. The sulfur content of hot gasified gas for a specially selected coal is 3,900 hours by volume of HjS and COS per million. At the temperature of the reaction and with a low content of CO2IH-O after mixing, the amount of sulfur in the gas leaving the desulfurizer is about 120 ppm. Million parts of the volume. This sulfur level is below the maximum and can be tolerated in the direct reduction of iron, so it is further reduced by mixing with a hot or cold reducing sulfur-free gas from conduit 46 or 47. The amount of lime required depends on the sulfur content of the coal. The amount of SALT formed in the desulfurator as a result of the reaction of sulfur with lime constitutes a small fraction of the total gas volume and has only a side effect on the quality of the gas coming out of the desulfuator from outlet line 35. CO separated out in the desulfurator by calcining limestone impact on gas quality. Side additions of HgO are included in the tables. In desulfurator 30, the shnhta leaves the reaction zoey and is cooled before unloading by introducing a relatively small stream of gas enriched in reducing agent from pipeline 38 to the gas cooler (High quality distribution element 39. The cooled high-quality gas flows upward and pushes towards the center of the reaction zone to the gas coming from the openings 33 and heated by a hot downwardly flowing down to the cooled zone. A portion of the gas enriched in the reducing agent is discharged from unit 27 to remove CO through water 28, L is introduced into gas heater 40 in the black: pipe 41. In the heater, which contains heating tubes 42 of heat-resistant alloy, the gas is heated to a temperature of about 815 s, which is preferable for directing the reduction of most types of iron oxide used as feed material. This temperature can be in the range between 7O-900 ° C without departing from the present invention. In the example, the gas leaving the desulfurator 30 through outlet pipe 35 after heating and firing the incoming cold limestone to produce calcined lime has a temperature of 915 ° C and is cooled down by supplying and mixing with a relatively small stream of gas, enriched with a reducing agent, from pipe 47. Adding gas enriched with a reducing agent through pipe 47 can be eliminated by simple heating in the heater 40 to a temperature less than in order to obtain a gas reducing mixture temperature of about 815 ° C in the inlet line 7 for the inlet of the reducing gas. With the help of an additional mixing gas flowing through conduit 47, it is easier to control the temperature of the hot reducing gas that enters the inlet line 7. The tables are based on producing one metric ton direct recovery of iron having a degree of metallization of 92% and carbon content 1.5%. In tab. 1 shows the gas flow rate and gas quality (the ratio of the reducing agent to the oxidizer) ri different places of the device.
Gas mixture to desul31 furator
Gas leaving note.
 The demand for raw material gasifier 5a 16 is coal, kg: Dry coal 488
93
H2O
Oxygen, (nm 98% 02) 235 The need for raw materials and the finished product of the desulphurizer 30 is, kg:
Famous for (input) 32.6 cao. (Release) 9.1
CaS (release) Ilf7
. Energy costs of the implementation of the proposed method, cal:
Gasification coal 3.1
Oxygen production
for coal gasification 0.4
 Approximately 140 kV “h at; 30% conversion efficiency. Both
In tab. 2 shows the gas temperature in the indicated places of the scheme ..
Table
1463
9.0
The results of gas analysis, while in the table. 3. Flow 6tra of the treated gas in the bypass 9 is less than the flow of reducing gas in the pipeline 7, since 1.5% of carbon is added to the directly removed iron as a result of reaction with CO from the reducing gas. Spent recovery 32 .024.1 27.0 gusher gas 9 35.126.5 29.6 Upper gas, concentrated gas, reducing agent 29 49.9 2/0 42.1
. The flow rate of gasified gas in line 19, as shown in the primure, is 931 nm per,: metric ton straight-reclaiming ... Melt iron. This: gas contains 85.5% or 796 of reducing agents (SSM-H). The flow rate of the hot reducing gas in the inlet master 7 is 19.9 nm, of which 88.6% or 1.44 nm are reducing agents SO-LH. Thus, only 4% () required for direct reduction in furnace 1 is supplied with a gasifier 16. The remaining 54% of the demand for leasing gas is the recirculation of exhaust gas from the direct reduction furnace.
Table3
Although in the proposed method for desulphurisation of gas, a de5 shaft-type sulfonator with countercurrent is used, it should be borne in mind that desulfur- ;. another type of rator, such as, for example, a fluidized bed of lime particles. Moreover, instead of lime, any other desulfuric acid agent can be used, for example, any other suitable sulfuric absorber, such as magnesium oxide.
The invention provides an energy and thermo-economical method for producing direct reduction of iron, using coal gasified gas as a source of reducing agent for direct reduction. 14.4 0.2 2.3 O 6.0 0.2 2.6 O 2.0 0.3 3.6 O
权利要求:
Claims (3)
[1]
1. METHOD FOR REMOVING IRON OXIDE, including reduction in a shaft furnace with a countercurrent material loaded from above and hot reducing gas, consisting of a mixture of recirculated and desulfurized gas from gasification of solid fuel with a quality index of at least 6.5, which is equal to in order to reduce heat costs, part of the recirculated reducing gas is added to the gasification obtained at the outlet of the gasifier in front of the desulfurizer, and the other part is heated to 760-900 ° C and mixed with Otoko coming from the desulfurizer, prior to feeding to the reduction zone.
>
[2]
2. The method according to π. ^ characterized in that a portion of the cold recycle gas is added before mixing with the heated portion.
[3]
3. The method according to π. 1, due to the fact that part of the cold recirculated gas is supplied to the cooling zone of the reactor for gas desulfurization.
The purpose of the invention is the reduction of heat costs.
This goal is achieved by the fact that according to the method of reducing iron oxide, which includes recovering in a shaft furnace a countercurrent material loaded from above and hot reducing gas, consisting of a mixture of recirculated and desulfurized gas from solid fuel gasification with a quality index of at least 6.5, a portion of the recirculated reducing gas is added to · Obtained by gasification at the outlet of the gasifier in front of the desulfator, and the other part is heated to 760-900 6 C and mixed with the flow going and h desulfurizer, before serving in the recovery zone. updates.
20 A portion of the cold recycle gas is added before mixing with the heated portion.
A portion of the cold recirculated gas is fed into the cooling zone of the reactor for desulfurization of the gas.
The drawing shows a diagram of the implementation of the method.
The diagram shows the furnace 1 with a fireproof coating of shaft type 30 with a counterflow of material and reducing agent. The feed material 2 (iron oxide) in the form of oxide pellets and / or large ore with a nominal size of. within 535 30 mm is fed into the feed hopper 3 of the willow furnace through the feed line 4 to create a mixture in the furnace. Reconstituted iron pellets and / or lump product are discharged from the lower zone of the furnace through the exhaust line 5 to the unloading conveyor 6, the speed of which is controlled 10
类似技术:
公开号 | 公开日 | 专利标题
SU1052165A3|1983-10-30|Method for reducing iron oxide
CA1108865A|1981-09-15|Method and apparatus for the direct reduction of ironore
US4539188A|1985-09-03|Process of afterburning and purifying process exhaust gases
US3920417A|1975-11-18|Method of gasifying carbonaceous material
US4260412A|1981-04-07|Method of producing direct reduced iron with fluid bed coal gasification
US4046557A|1977-09-06|Method for producing metallic iron particles
US4613344A|1986-09-23|Method and apparatus for cleaning hot gases produced during a coal gasification process
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SU938747A3|1982-06-23|Process and apparatus for reducing iron oxide and producing molten crude iron
KR900006603B1|1990-09-13|Process for the direct reduction of iron-oxide-containing materials
US4201571A|1980-05-06|Method for the direct reduction of iron and production of fuel gas using gas from coal
US4685964A|1987-08-11|Method and apparatus for producing molten iron using coal
US3909244A|1975-09-30|Process for directly reducing iron ores in the solid state under pressure
AU701539B2|1999-01-28|Process for producing sponge iron and plant for carrying out the process
US4331470A|1982-05-25|Method for the direct reduction of iron in a shaft furnace using gas from coal
SU1711677A3|1992-02-07|Method and apparatus for production melted pig iron or intermediately product for steel making
US5542963A|1996-08-06|Direct iron and steelmaking
US4439233A|1984-03-27|Direct reduction of iron
US4234169A|1980-11-18|Apparatus for the direct reduction of iron and production of fuel gas using gas from coal
US4365789A|1982-12-28|Apparatus for the direct reduction of iron in a shaft furnace using gas from coal
US4225340A|1980-09-30|Method for the direct reduction of iron using gas from coal
EP0657550A1|1995-06-14|Method and apparatus for producing iron
US4205830A|1980-06-03|Apparatus for the direct reduction of iron using gas from coal
US4049440A|1977-09-20|Method for producing metallic iron pellets
同族专利:
公开号 | 公开日
PL217733A1|1980-05-05|
AU523276B2|1982-07-22|
AT367456B|1982-07-12|
BE878154A|1979-12-03|
YU40934B|1986-08-31|
AU4978879A|1980-02-21|
DE2932939A1|1980-02-28|
SE436760B|1985-01-21|
TR20764A|1982-07-01|
ATA552979A|1981-11-15|
BR7905180A|1980-04-29|
PT70059A|1979-09-01|
AR218150A1|1980-05-15|
PL120142B1|1982-02-27|
DE2932939C2|1987-10-01|
JPS5528395A|1980-02-28|
CA1118211A|1982-02-16|
IN152255B|1983-11-26|
JPS6233284B2|1987-07-20|
YU196879A|1982-10-31|
PH14399A|1981-06-25|
GR70352B|1982-09-24|
GB2027741A|1980-02-27|
LU81597A1|1979-12-07|
CS218587B2|1983-02-25|
NL7906187A|1980-02-19|
SE7906809L|1980-02-16|
MX152098A|1985-05-29|
ES483373A1|1980-04-16|
IT1122470B|1986-04-23|
ZA793867B|1980-08-27|
FR2433580B1|1984-01-27|
FI792271A|1980-02-16|
NZ191204A|1980-11-14|
MA18563A1|1980-04-01|
IT7925044D0|1979-08-10|
FR2433580A1|1980-03-14|
US4173465A|1979-11-06|
GB2027741B|1982-07-14|
引用文献:
公开号 | 申请日 | 公开日 | 申请人 | 专利标题

US3853538A|1973-07-20|1974-12-10|Steel Corp|Use of reducing gas by coal gasification for direct iron ore reduction|
US3844766A|1973-12-26|1974-10-29|Midland Ross Corp|Process for reducing iron oxide to metallic sponge iron with liquid or solid fuels|
DE2438790B2|1974-08-13|1976-09-09|Thyssen Purofer GmbH, 4000 Düsseldorf|PROCESS AND SYSTEM FOR THE REDUCTION OF IRON ORES, IN PARTICULAR IRON ORES PELLETS|
DE2459876B1|1974-12-18|1976-06-24|Thyssen Purofer Gmbh|PLANT FOR THE DIRECT REDUCTION OF IRON ORES|
JPS5917163B2|1976-01-14|1984-04-19|Mitsubishi Heavy Ind Ltd|US4260412A|1980-01-16|1981-04-07|Midrex Corporation|Method of producing direct reduced iron with fluid bed coal gasification|
US4331470A|1980-09-15|1982-05-25|Midrex Corporation|Method for the direct reduction of iron in a shaft furnace using gas from coal|
DE3104281C2|1981-02-07|1985-10-31|SKF Steel Engineering AB, Hofors|Method and device for the production of sponge iron|
DE3104405C2|1981-02-07|1985-10-31|SKF Steel Engineering AB, Hofors|Plant and process for the production of sponge iron|
JPH0548365Y2|1983-07-20|1993-12-24|
AT382165B|1983-08-18|1987-01-26|Voest Alpine Ag|METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS AND DEVICE FOR IMPLEMENTING THE METHOD|
US4608240A|1983-11-04|1986-08-26|Hylsa, S.A.|Method for the desulfurization of hydrocarbon gas|
IT1177075B|1983-12-02|1987-08-26|Skf Steel Eng Ab|PROCEDURE AND PLANT TO REDUCE OXIDE MATERIAL|
IT1177076B|1983-12-02|1987-08-26|Skf Steel Eng Ab|PROCESS AND PLANT TO REDUCE OXIDE MATERIAL SIMULTANEOUSLY GENERATING A GAS SUITABLE FOR THE RECOVERY OF THERMAL ENERGY|
IT1177077B|1983-12-02|1987-08-26|Skf Steel Eng Ab|PROCEDURE AND PLANT TO REDUCE OXIDE MATERIAL SIMULTANEOUSLY GENERATING A GAS SUITABLE AS COMBUSTIBLE GAS|
AT381954B|1984-08-16|1986-12-29|Voest Alpine Ag|METHOD FOR DIRECTLY REDUCING IRON OXIDE MATERIALS|
GB2191782A|1986-06-17|1987-12-23|Midrex Int Bv|Method and apparatus for producing upgraded synthetic fuel gas from coal|
GB9123369D0|1991-11-04|1991-12-18|Boc Group Plc|Separation of hydrogen|
AT406484B|1995-08-16|2000-05-25|Voest Alpine Ind Anlagen|METHOD FOR THE PRODUCTION OF LIQUID PIG IRON OR LIQUID STEEL PRE-PRODUCTS AND SPONGE OF IRON, AND SYSTEM FOR IMPLEMENTING THE METHOD|
US6149859A|1997-11-03|2000-11-21|Texaco Inc.|Gasification plant for direct reduction reactors|
JP3939492B2|2000-11-08|2007-07-04|株式会社神戸製鋼所|Coal gasification direct reduction iron making|
AT505490B1|2007-06-28|2009-12-15|Siemens Vai Metals Tech Gmbh|METHOD AND DEVICE FOR PRODUCING IRON SPONGE|
CN101910375B|2007-12-28|2014-11-05|格雷特波因特能源公司|Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock|
CA2716135C|2008-02-29|2013-05-28|Greatpoint Energy, Inc.|Particulate composition for gasification, preparation and continuous conversion thereof|
WO2009111332A2|2008-02-29|2009-09-11|Greatpoint Energy, Inc.|Reduced carbon footprint steam generation processes|
US8652222B2|2008-02-29|2014-02-18|Greatpoint Energy, Inc.|Biomass compositions for catalytic gasification|
US8366795B2|2008-02-29|2013-02-05|Greatpoint Energy, Inc.|Catalytic gasification particulate compositions|
US8286901B2|2008-02-29|2012-10-16|Greatpoint Energy, Inc.|Coal compositions for catalytic gasification|
US8297542B2|2008-02-29|2012-10-30|Greatpoint Energy, Inc.|Coal compositions for catalytic gasification|
CN102159683B|2008-09-19|2014-10-01|格雷特波因特能源公司|Processes for gasification of carbonaceous feedstock|
US8502007B2|2008-09-19|2013-08-06|Greatpoint Energy, Inc.|Char methanation catalyst and its use in gasification processes|
US8328890B2|2008-09-19|2012-12-11|Greatpoint Energy, Inc.|Processes for gasification of a carbonaceous feedstock|
WO2010078298A1|2008-12-30|2010-07-08|Greatpoint Energy, Inc.|Processes for preparing a catalyzed coal particulate|
US8734547B2|2008-12-30|2014-05-27|Greatpoint Energy, Inc.|Processes for preparing a catalyzed carbonaceous particulate|
LU91547B1|2009-04-03|2010-10-04|Wurth Paul Sa|Method and installation for producing direct reduced iron|
US8728182B2|2009-05-13|2014-05-20|Greatpoint Energy, Inc.|Processes for hydromethanation of a carbonaceous feedstock|
JP5269251B2|2009-05-13|2013-08-21|グレイトポイント・エナジー・インコーポレイテッド|Process for the hydrogenation methanation of carbonaceous feedstock|
AT508291B1|2009-05-28|2011-07-15|Siemens Vai Metals Tech Gmbh|METHOD AND DEVICE FOR REDUCING OXIDIC ICE CARRIER WITH REDUCTION GAS FROM A CARBURETOR|
US20110031439A1|2009-08-06|2011-02-10|Greatpoint Energy, Inc.|Processes for hydromethanation of a carbonaceous feedstock|
JP5771615B2|2009-09-16|2015-09-02|グレイトポイント・エナジー・インコーポレイテッド|Hydrogenation methanation process of carbonaceous feedstock|
WO2011034890A2|2009-09-16|2011-03-24|Greatpoint Energy, Inc.|Integrated hydromethanation combined cycle process|
CN102482598B|2009-09-16|2014-09-17|格雷特波因特能源公司|Two-mode process for hydrogen production|
WO2011034889A1|2009-09-16|2011-03-24|Greatpoint Energy, Inc.|Integrated hydromethanation combined cycle process|
CA2773845C|2009-10-19|2014-06-03|Greatpoint Energy, Inc.|Integrated enhanced oil recovery process|
AU2010310846B2|2009-10-19|2013-05-30|Greatpoint Energy, Inc.|Integrated enhanced oil recovery process|
WO2011084580A2|2009-12-17|2011-07-14|Greatpoint Energy, Inc.|Integrated enhanced oil recovery process|
CN102754266B|2010-02-23|2015-09-02|格雷特波因特能源公司|integrated hydrogenation methanation fuel cell power generation|
US8652696B2|2010-03-08|2014-02-18|Greatpoint Energy, Inc.|Integrated hydromethanation fuel cell power generation|
EP2563883A1|2010-04-26|2013-03-06|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock with vanadium recovery|
KR101506381B1|2010-05-28|2015-03-26|그레이트포인트 에너지, 인크.|Conversion of liquid heavy hydrocarbon feedstocks to gaseous products|
US8748687B2|2010-08-18|2014-06-10|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock|
WO2012033997A1|2010-09-10|2012-03-15|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock|
EP2635660A1|2010-11-01|2013-09-11|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock|
WO2012061235A1|2010-11-01|2012-05-10|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock|
CN103391989B|2011-02-23|2015-03-25|格雷特波因特能源公司|Hydromethanation of a carbonaceous feedstock with nickel recovery|
CN103492537A|2011-04-22|2014-01-01|格雷特波因特能源公司|Hydromethanation of a carbonaceous feedstock with char beneficiation|
WO2012166879A1|2011-06-03|2012-12-06|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock|
CN103890148A|2011-08-17|2014-06-25|格雷特波因特能源公司|Hydromethanation of a carbonaceous feedstock|
US20130042824A1|2011-08-17|2013-02-21|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock|
IN2014CN02080A|2011-08-20|2015-05-29|Hyl Technologies Sa De Cv|
US9012524B2|2011-10-06|2015-04-21|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock|
WO2014055353A1|2012-10-01|2014-04-10|Greatpoint Energy, Inc.|Agglomerated particulate low-rank coal feedstock and uses thereof|
KR101576781B1|2012-10-01|2015-12-10|그레이트포인트 에너지, 인크.|Agglomerated particulate low-rank coal feedstock and uses thereof|
KR101646890B1|2012-10-01|2016-08-12|그레이트포인트 에너지, 인크.|Agglomerated particulate low-rank coal feedstock and uses thereof|
US9328920B2|2012-10-01|2016-05-03|Greatpoint Energy, Inc.|Use of contaminated low-rank coal for combustion|
US10464872B1|2018-07-31|2019-11-05|Greatpoint Energy, Inc.|Catalytic gasification to produce methanol|
US10344231B1|2018-10-26|2019-07-09|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock with improved carbon utilization|
US10435637B1|2018-12-18|2019-10-08|Greatpoint Energy, Inc.|Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation|
US10618818B1|2019-03-22|2020-04-14|Sure Champion Investment Limited|Catalytic gasification to produce ammonia and urea|
法律状态:
优先权:
申请号 | 申请日 | 专利标题
US05/933,691|US4173465A|1978-08-15|1978-08-15|Method for the direct reduction of iron using gas from coal|
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