CN115125347A - Preparation method of gas-based shaft furnace reducing gas by taking hydrocarbon-rich gas as raw material gas - Google Patents
Preparation method of gas-based shaft furnace reducing gas by taking hydrocarbon-rich gas as raw material gas Download PDFInfo
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- CN115125347A CN115125347A CN202210884791.3A CN202210884791A CN115125347A CN 115125347 A CN115125347 A CN 115125347A CN 202210884791 A CN202210884791 A CN 202210884791A CN 115125347 A CN115125347 A CN 115125347A
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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- C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
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- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
- C01B2203/0255—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a non-catalytic partial oxidation step
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Abstract
The invention discloses a preparation method of gas-based shaft furnace reducing gas by taking hydrocarbon-rich gas as raw material gas, belonging to the field of direct reduction. Preheating a first hydrocarbon-rich gas to 250-700 ℃, then feeding the first hydrocarbon-rich gas into a non-catalytic partial oxidation converter, combusting the first hydrocarbon-rich gas with pure oxygen to perform partial oxidation reaction, controlling the combustion temperature to enable the temperature of a reducing gas at an outlet of the converter to be 1100-1200 ℃, then mixing a second hydrocarbon-rich gas or purified gas decarbonized at the top of a gas-based shaft furnace into the reducing gas at an outlet pipeline of the converter to form a mixed gas at the temperature of 850-1100 ℃, and feeding the mixed gas into the gas-based shaft furnace from a tuyere of the gas-based shaft furnace. The invention solves the problem of high water content in high-temperature reducing gas produced by a non-catalytic partial oxidation process by improving the preheating temperature of the hydrocarbon-rich gas and mixing the preheated hydrocarbon-rich gas into an outlet pipeline of a non-catalytic furnace, and provides a method for preparing gas-based shaft furnace reducing gas by using the non-catalytic partial oxidation process.
Description
Technical Field
The invention belongs to the field of direct reduction, and particularly relates to a preparation method of gas-based shaft furnace reducing gas by taking hydrocarbon-rich gas as raw material gas.
Background
At present, the raw materials for preparing the reducing gas of the gas-based shaft furnace are mainly hydrocarbon-rich gas and top circulating gas (CO + H) of the gas-based shaft furnace 2 ) The existing process for preparing the reducing gas from the hydrocarbon-rich gas comprises dry reforming, wet reforming and a non-catalytic partial oxidation method, and one requirement of the gas-based shaft furnace on the component of the reducing gas is CO 2 +H 2 O not more than 10 percent, and CO in reducing gas 2 +H 2 The lower the O content, the better. However, the production of the reducing gas from the hydrocarbon-rich gas requires the addition of an oxidant (e.g., CO) 2 、H 2 O、O 2 ) This will increase the CO content of the reducing gas 2 +H 2 O content, especially in reducing gas produced by non-catalytic partial oxidation, CO 2 +H 2 O is up toMore than 15 percent.
As noted in patent CN201280023094.3, an exemplary embodiment entitled "system and method for reducing iron oxide to metallic iron using coke oven gas and oxygen steelmaking furnace gas," reformed COG has the following exemplary contents: 2-13% CH4 (at about 1,500 degrees Celsius to about 1,200 degrees Celsius, respectively), 18.7% CO, 1.7% CO2, 43.4% H2, 17.7% H2O, 3.6% N2, and 1.8% C2H6, and possibly 0.9% C2H4 and 1.7% C2H 2. ", from this component, CO + H can be calculated 2 19.4 percent of O, which is far higher than the requirement index of the gas-based shaft furnace for reducing gas: CO2 2 +H 2 O is not more than 10 percent, so the technical scheme of the patent at least influences the productivity and the metallization rate of products and increases the energy consumption per ton of iron.
For another example, CN202110960672.7, entitled direct reduction method for producing sponge iron by converting hydrocarbon-rich gas, proposes in the examples that "the decarbonized gas is preheated in the waste heat recovery device 1, enters into the heating device 5 to perform partial oxidation combustion reaction with oxygen (preheated to about 240 ℃ in an oxygen heater 6), is further heated to about 700 ℃ (temperature is adjusted according to the required fresh reducing gas three temperature of the shaft furnace), and is mixed with the high-temperature reducing gas (1400 ℃) from the converter 2 (after mixing, the temperature is about 1050 ℃, and the ratio of the total volume of CO and H2 to the total volume of CO2 and H2O is greater than 10) to form fresh reducing gas three for reduction in the shaft furnace to produce sponge iron. ", as a general knowledge, the skilled person will know that CO2+ H in the high temperature reducing gas at 1400 ℃ formed by the partial oxidation combustion of a hydrocarbon-rich gas 2 O accounts for about 20%, and the main components of the decarbonized gas are CO and H2, which can increase CO when partially combusted with oxygen 2 +H 2 The content of O is equivalent to that of the previous decarburization and dehydration process, and the mixing of the two gases cannot achieve the purpose that the ratio of the total volume of CO and H2 to the total volume of CO2 and H2O is more than 10, which is proposed by the inventor of the patent.
Disclosure of Invention
In order to solve the technical problem, the invention provides a method for preparing gas-based shaft furnace reducing gas by taking hydrocarbon-rich gas as raw material gas.
One of the purposes of the invention is to solve the problem that the water content of high-temperature reducing gas produced by a non-catalytic partial oxidation conversion process in a gas-based shaft furnace is high, so that the total content of CO2+ H2O entering the gas-based shaft furnace is high.
The second purpose of the invention is to improve the metallization rate of the gas-based shaft furnace DRI for preparing reducing gas by adopting a non-catalytic partial oxidation conversion process.
The third purpose of the invention is to avoid using a high-temperature tube furnace (the working temperature of the outer wall of the tube is about 1100 ℃) to heat the reducing gas or the raw material gas, thereby not only reducing the investment cost of the gas heating furnace, but also avoiding the carbon precipitation blocking pipelines which are easily generated by carbon-containing gas, oxidizing gas and hydrogen in the reducing gas or the raw material gas under the high-temperature condition, and the hazards of carburizing, oxidizing and hydrogen corrosion to the tube wall.
Other objects of the present invention will be pointed out hereinafter or will be apparent to those skilled in the art.
In order to realize the purpose, the method adopts the following technical scheme:
a method for preparing reducing gas of a gas-based shaft furnace by taking rich hydrocarbon gas as raw material gas comprises the steps of pressurizing the raw material gas, heating the raw material gas by a heating furnace to prepare the reducing gas required by the gas-based shaft furnace, and feeding the reducing gas into the gas-based shaft furnace from a tuyere of the gas-based shaft furnace, wherein the method comprises the following steps: preheating the first hydrocarbon-rich gas to 250-700 ℃, then feeding the first hydrocarbon-rich gas into a non-catalytic partial oxidation converter, combusting the first hydrocarbon-rich gas with pure oxygen to perform partial oxidation reaction, controlling the combustion temperature to enable the temperature of reducing gas at an outlet of the converter to be 1100-1200 ℃, then mixing the second hydrocarbon-rich gas or purified gas decarbonized at the top of a gas-based shaft furnace into the reducing gas at an outlet pipeline of the converter to form mixed gas at the temperature of 850-1100 ℃, and feeding the mixed gas into the gas-based shaft furnace from a tuyere of the gas-based shaft furnace.
Compared with the prior art, the method has the following beneficial effects:
(1) in the prior art of chemical engineering, the preheating temperature of the hydrocarbon-rich gas is usually not more than 200 ℃ before entering the non-catalytic partial oxidation converter. The invention applies the technology in the chemical field to the metallurgy field, and the hydrocarbon-rich gas enters a non-catalytic partial converter to be combusted with pure oxygen by raising the preheating temperature of the hydrocarbon-rich gas to 250-700 ℃. Compared with the prior art in the chemical field, the oxygen consumption is reduced under the condition of reaching the same temperature of the converter outlet reducing gas, so that the content of CO2+ H2O in the converter outlet reducing gas is reduced, and the components of the non-catalytic partial oxidation converter outlet reducing gas meet the technical requirements in the metallurgical field; in addition, the content of CO2+ H2O in the purified gas obtained by decarbonizing the top of the gas-based shaft furnace or the hydrocarbon-rich gas is controllable, so that the content of CO2+ H2O in the mixed gas can be further reduced by mixing the hydrocarbon-rich gas or the purified gas obtained by decarbonizing the top of the gas-based shaft furnace into the reducing gas of the outlet pipeline of the converter, and the combustion temperature of the converter is controlled, so that the content of CO2+ H2O in the reducing gas entering the gas-based shaft furnace is in the range of 6-10%, and the requirement of the gas-based shaft furnace on the reducing gas entering the converter is met.
(2) The hydrocarbon components in the reducing gas entering the gas-based shaft furnace are increased due to the mixing of the hydrocarbon-rich gas, and the hydrocarbon components can react with water to generate H2 and CO under the catalysis of direct reduced iron in the gas-based shaft furnace, so that the total amount of the reducing gas is increased, the water content is reduced, and the improvement of the metallization rate of DRI in the gas-based shaft furnace is facilitated.
(3) The carbon content of the direct reduced iron product can be increased by adding the hydrocarbon-rich gas, and the increased carbon content of the direct reduced iron can increase the oxidation resistance of the direct reduced iron and reduce the power consumption of the subsequent electric furnace melting separation.
(4) The upper limit of the temperature of the tubular furnace for heating the hydrocarbon-rich gas is 700 ℃, and a high-temperature tubular furnace (the working temperature of the outer wall of the tube is about 1100 ℃) is not needed, so that the investment of the heating furnace is reduced, and the hidden trouble in the running process of the high-temperature tubular furnace is avoided.
The method adopts the following two preferable schemes:
the first scheme is as follows: preheating the first hydrocarbon-rich gas to 250-350 ℃, then entering a non-catalytic partial oxidation converter, and combusting with pure oxygen.
The second scheme is as follows: preheating the first hydrocarbon-rich gas to 500-700 ℃, and then feeding the first hydrocarbon-rich gas into a non-catalytic partial oxidation converter to be combusted with pure oxygen.
Further, in each of the above embodiments, the second hydrocarbon-rich gas is preheated to a certain temperature and then mixed into the reducing gas in the outlet pipeline of the reformer.
Further, in the first scheme, the second hydrocarbon-rich gas is preheated to 250-350 ℃ and then mixed into the reducing gas of the outlet pipeline of the reformer.
Further, in the first scheme, the preheating temperature of the first hydrocarbon-rich gas and the second hydrocarbon-rich gas is 280-300 ℃.
Further, in the second scheme, the second hydrocarbon-rich gas is preheated to 500-700 ℃ and then mixed into the reducing gas of the outlet pipeline of the reformer.
Further, in the second scheme, the preheating temperature of the first hydrocarbon-rich gas and the second hydrocarbon-rich gas is 600-700 ℃.
Further, when the first hydrocarbon-rich gas and the second hydrocarbon-rich gas are preheated to more than 500 ℃, unsaturated hydrocarbons in the hydrocarbon-rich gas need to be converted into saturated hydrocarbons.
Further, in the second scheme, before preheating the first hydrocarbon-rich gas and the second hydrocarbon-rich gas, organic sulfur in the hydrocarbon-rich gas needs to be converted into H2S.
Compared with the prior art, the optimal selection method has the following beneficial effects:
(1) the first scheme mainly aims at the hydrocarbon-rich gas containing complex hydrocarbon, such as coke oven gas and the like, and adopts the preheating temperature (200 ℃) higher than that of the chemical field and the preheating temperature (350 ℃) lower than that of the carbon deposition of the complex hydrocarbon, so that the moisture in the reducing gas generated by the non-catalytic partial oxidation process of the hydrocarbon-rich gas can be reduced, and the carbon deposition generated at the overhigh preheating temperature can be avoided. Meanwhile, a device for converting unsaturated hydrocarbons in the hydrocarbon-rich gas into saturated hydrocarbons is not required to be added, so that the equipment investment is reduced.
(2) In the second scheme, the hydrocarbon-rich gas is preheated to 500-700 ℃, preferably 600-700 ℃, and then enters the non-catalytic partial converter, and the combustion temperature of the converter is controlled, so that the temperature of the reducing gas at the outlet of the converter is 1100 ℃, at the moment, the content of H2O in the reducing gas at the outlet of the converter is about 5.5-6.5%, and the content of (H2O + CO2) is about 6.8-8.0%, which is lower than the content of (H2O + CO2) in the reducing gas in the prior art, or is similar to the content of (H2O + CO2) in the prior art, so that the hydrocarbon-rich gas is superior to the reducing gas component prepared in the prior art, or is equivalent to the reducing gas component prepared in the prior art. In order to preheat the hydrocarbon-rich gas to 500-700 ℃ without carbon deposition, a treatment method of converting unsaturated hydrocarbon in the hydrocarbon-rich gas into saturated hydrocarbon and converting organic sulfur in the hydrocarbon-rich gas into H2S is adopted, so that the hydrocarbon-rich gas containing complex hydrocarbon and organic sulfur, such as coke oven gas, can be preheated to 600-700 ℃ without carbon deposition, and conditions are created for reducing oxygen consumption of a subsequent non-catalytic partial oxidation process.
(3) Along with the increase of the preheating temperature of the second hydrocarbon-rich gas, the amount of the second hydrocarbon-rich gas mixed into the reducing gas of the outlet pipeline of the reformer is increased, the content of H2O + CO2 in the reducing gas entering the gas-based shaft furnace is lower, and the effective reducing gas component is higher.
Drawings
FIG. 1 is a schematic view of a first process flow of the present invention;
FIG. 2 is a schematic view of a second process flow of the present invention;
FIG. 3 is a schematic view of a third process flow of the present invention;
labeled in the figure as: 1-gas-based shaft furnace, 11-gas-based shaft furnace top hot gas outlet pipeline, 12-gas-based shaft furnace tuyere, 13-shaft furnace hot gas heat exchanger, 14-dust removal device, 15-dehydration device, 16-shaft furnace top gas compressor, 17-desulfurization device, 18-CO removal 2 The device comprises a 111-gas-based shaft furnace top first gas flow pipeline, a 112-gas-based shaft furnace top second gas flow pipeline, a 2-non-catalytic partial oxidation reformer, a 21-non-catalytic partial oxidation reformer outlet pipeline, a 22-top burner of the non-catalytic partial oxidation reformer, a 3-preheating furnace, a 4-hydrocarbon-rich gas source, a 41-first hydrocarbon-rich gas pipeline, a 42-second hydrocarbon-rich gas pipeline, a 43-hydrogen-rich gas compressor, a 5-steam pipeline, a 6-oxygen pipeline, a 7-mixed reduction gas pipeline and an 8-iron-molybdenum hydrogenation converter.
Detailed Description
The present invention will be described in detail with reference to the following embodiments in order to fully understand the objects, features and effects of the invention, but the present invention is not limited thereto.
The first embodiment is as follows: the present embodiment is described with reference to fig. 1 to fig. 3, and the method for preparing reducing gas of a gas-based shaft furnace using rich hydrocarbon gas as raw material gas in the present embodiment includes steps of pressurizing raw material gas from a rich hydrocarbon gas source by a compressor, heating the raw material gas by a heating furnace to prepare reducing gas required by the gas-based shaft furnace, and introducing the reducing gas into the gas-based shaft furnace from a tuyere of the gas-based shaft furnace, wherein: after preheating, the hydrocarbon-rich gas in the first hydrocarbon-rich gas pipeline 41 reaches 250-700 ℃, then enters the non-catalytic partial oxidation converter 2 through the burner 22, is combusted with pure oxygen introduced through the oxygen pipeline 6 to generate partial oxidation reaction, the combustion temperature is controlled to enable the temperature of the reducing gas in the outlet pipeline 21 of the converter 2 to be 1100-1200 ℃, then the hydrocarbon-rich gas in the second hydrocarbon-rich gas pipeline 42 or the gas-based shaft furnace top purified coal gas after passing through the CO2 removing device 18 is mixed into the reducing gas in the outlet pipeline 21 of the converter 2 to become mixed reducing gas with the temperature of 850-1100 ℃, and the mixed reducing gas enters the gas-based shaft furnace 1 from the gas-based shaft furnace tuyere 12 through the mixed reducing gas pipeline 7.
The second embodiment is as follows: referring to fig. 1 to 3, a method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas according to the present embodiment will be described, in which: after preheating, the hydrocarbon-rich gas in the first hydrocarbon-rich gas pipeline 41 enters the non-catalytic partial oxidation converter 2 through the burner 22 after the temperature of the hydrocarbon-rich gas reaches 250-350 ℃, and is combusted with pure oxygen. Technical features not disclosed in the present embodiment are the same as those of the first embodiment.
The third concrete implementation mode: the present embodiment will be described with reference to fig. 1 to 3, which illustrate a method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas, in which: after preheating, the hydrocarbon-rich gas in the first hydrocarbon-rich gas pipeline 41 enters the non-catalytic partial oxidation converter 2 through the burner 22 after the temperature of the hydrocarbon-rich gas reaches 500-700 ℃, and is combusted with pure oxygen. Technical features not disclosed in the present embodiment are the same as those of the first embodiment.
The fourth concrete implementation mode: referring to fig. 1 to 3, a method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas according to the present embodiment will be described, in which: after preheating to a certain temperature, the hydrocarbon-rich gas in the second hydrocarbon-rich gas line 42 is mixed into the reducing gas in the reformer outlet line 21. The technical features not disclosed in this embodiment are the same as those of the first, second or third embodiment.
The fifth concrete implementation mode: the present embodiment will be described with reference to fig. 1 to 3, which illustrate a method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas, in which: after preheating, the hydrocarbon-rich gas in the second hydrocarbon-rich gas pipeline 42 is mixed into the reducing gas in the reformer outlet pipeline 21 after reaching 250-350 ℃. The technical features not disclosed in the present embodiment are the same as those of the second embodiment.
The sixth specific implementation mode is as follows: in the method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas according to the present embodiment, the hydrocarbon-rich gas in the first hydrocarbon-rich gas line 41 and the second hydrocarbon-rich gas line 42 after preheating has a temperature of 280 to 300 ℃. The technical features not disclosed in the present embodiment are the same as those in the fifth embodiment.
The seventh embodiment: referring to fig. 1 to 3, a method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas according to the present embodiment will be described, in which: after preheating, the hydrocarbon-rich gas in the second hydrocarbon-rich gas pipeline 42 is mixed into the reducing gas in the reformer outlet pipeline 21 after the temperature of the hydrocarbon-rich gas reaches 500-700 ℃. The technical features not disclosed in the present embodiment are the same as those of the third embodiment.
The specific implementation mode is eight: referring to fig. 1 to 3, a method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas according to the present embodiment will be described, in which: after preheating, the hydrocarbon-rich gas temperature in the first hydrocarbon-rich gas pipeline 41 and the second hydrocarbon-rich gas pipeline 42 is 600-700 ℃. The technical features not disclosed in this embodiment are the same as those in the seventh embodiment.
The specific implementation method nine: referring to fig. 1 to 3, a method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas according to the present embodiment will be described, in which: when the hydrocarbon-rich gas in the first hydrocarbon-rich gas line 41 and the second hydrocarbon-rich gas line 42 is preheated to a temperature of 500 ℃ or higher, unsaturated hydrocarbons in the hydrocarbon-rich gas are converted into saturated hydrocarbons. The technical features not disclosed in this embodiment are the same as those of the first or third or seventh or eighth embodiment.
The detailed implementation mode is ten: referring to fig. 1 to 3, a method for producing a gas-based shaft furnace reducing gas using a hydrocarbon-rich gas as a raw material gas according to the present embodiment will be described, in which: before preheating the hydrocarbon-rich gas in the first hydrocarbon-rich gas line 41 and the second hydrocarbon-rich gas line 42, the organic sulfur in the hydrocarbon-rich gas is converted into H2S. Technical features not disclosed in the present embodiment are the same as those in the ninth embodiment.
Example one
The present embodiment will be described with reference to fig. 1.
FIG. 1 is a schematic view of a first process of the present invention.
The embodiment of the invention discloses a preparation method of gas-based shaft furnace reducing gas by taking hydrocarbon-rich gas as raw material gas, which comprises the following steps: pressurizing hydrocarbon-rich gas of a hydrocarbon-rich gas source 4 by a compressor 43, heating by using an external combustion tube type preheating furnace 3, and when the hydrocarbon-rich gas is natural gas, heating to 500-700 ℃, preferably to 600-700 ℃; when the hydrocarbon-rich gas is coke oven gas, the temperature is heated to 250-350 ℃, preferably 280-300 ℃. The outlet of the preheating furnace 3 is divided into two pipelines, namely a first hydrocarbon-rich gas pipeline 41 and a second hydrocarbon-rich gas pipeline 42, the outlet of the first hydrocarbon-rich gas pipeline 41 is communicated with the inlet of a top burner 22 of the non-catalytic partial oxidation reforming furnace 2, an oxygen pipeline 6 is communicated with the top burner 22 of the non-catalytic partial oxidation reforming furnace 2 after passing through a gas-based shaft furnace top gas heat exchanger 13, a steam pipeline 5 is communicated with the top burner 22 of the non-catalytic partial oxidation reforming furnace 2, the hydrocarbon-rich gas and pure oxygen are combusted in the non-catalytic partial oxidation reforming furnace to generate partial oxidation reaction, the combustion temperature is controlled to enable the temperature of the reducing gas in the outlet pipeline 21 of the reforming furnace 2 to be 1100-1200 ℃, then the outlet pipeline 21 of the reforming furnace and the second hydrocarbon-rich gas pipeline 42 are connected in parallel to form a mixed reducing gas pipeline 7, and the outlet of the mixed gas reducing gas pipeline 7 is communicated with the tuyere 12 of the gas-based shaft furnace 1. And controlling the flow rate of the hydrocarbon-rich gas in the second hydrocarbon-rich gas pipeline 42 to ensure that the temperature of the mixed reducing gas in the mixed reducing gas pipeline 7 is 850-1100 ℃. The top gas of the gas-based shaft furnace 1 sequentially passes through a top hot gas outlet pipeline 11 of the gas-based shaft furnace, a shaft furnace hot gas heat exchanger 13 and a dust removal device 14 and then enters a gas pipe network for other purposes.
Example two
The present embodiment is described below with reference to fig. 2: the hydrocarbon-rich gas source 4 is coke oven gas, the coke oven gas is firstly pre-purified, then is pressurized by a compressor 43, and is preheated to 280 ℃ by using convection section hot flue gas of a preheating furnace 3, then enters an iron-molybdenum hydrogenation converter 8, unsaturated hydrocarbon in the coke oven gas is converted into saturated hydrocarbon and organic sulfur is converted into H2S in the iron-molybdenum hydrogenation converter 8, and is desulfurized by a desulfurizing tank, the coke oven gas enters the preheating furnace 3 and is heated to 500-700 ℃, preferably to 600-700 ℃, two pipelines are divided into a first hydrocarbon-rich gas pipeline 41 and a second hydrocarbon-rich gas pipeline 42 at the outlet of the preheating furnace 3, the outlet of the first hydrocarbon-rich gas pipeline 41 is communicated with the inlet of a burner 22 at the top of the non-catalytic partial oxidation converting furnace 2, an oxygen pipeline 6 is communicated with the burner 22 at the top of the non-catalytic partial oxidation converting furnace 2 after passing through a gas heat exchanger 13 of a gas-based shaft furnace, a steam pipeline 5 is communicated with the burner 22 at the top of the non-catalytic partial oxidation converting furnace 2, in a non-catalytic partial oxidation converter, coke oven gas and pure oxygen are combusted to generate partial oxidation reaction, the combustion temperature is controlled to enable the temperature of reducing gas in an outlet pipeline 21 of a converter 2 to be 1100-1200 ℃, then the outlet pipeline 21 of the converter and a second hydrocarbon-rich gas pipeline 42 are connected in parallel to form a mixed reducing gas pipeline 7, and the outlet of the mixed reducing gas pipeline 7 is communicated with a tuyere 12 of a gas-based shaft furnace 1. Controlling the flow rate of the coke oven gas in the second hydrocarbon-rich gas pipeline 42 to make the temperature of the mixed reducing gas in the mixed reducing gas pipeline 7 be 850-1100 ℃. The top gas of the gas-based shaft furnace 1 sequentially passes through a top hot gas outlet pipeline 11 of the gas-based shaft furnace, a hot gas heat exchanger 13 of the shaft furnace and a dust removal device 14 and then enters a gas pipe network for other purposes.
EXAMPLE III
The present embodiment is explained below with reference to fig. 3: the difference between the method for preparing the gas-based shaft furnace reducing gas by using the hydrocarbon-rich gas as the raw material gas in the embodiment and the second embodiment is that the outlet of the preheating furnace 3 is only communicated with a first hydrocarbon-rich gas pipeline 41; after passing through a top hot gas outlet pipeline 11, a shaft furnace hot gas heat exchanger 13 and a dust removal device 14 in sequence, top gas of a gas-based shaft furnace 1 is divided into two gas flow pipelines, wherein the first gas flow pipeline is 111, the second gas flow pipeline is 112, the second gas flow is used for other purposes, and the first gas flow pipeline is used for other purposes111 is then sequentially connected with a dehydration device 15, a shaft furnace top gas compressor 16, a desulfurization device 17 and a CO removal device 2 The devices 18 are communicated and remove CO 2 The gas flowing out of the outlet of the device 18 is gas-based shaft furnace top purified gas, the main components of the gas-based shaft furnace top purified gas are H2 and CO, and H 2 O+CO 2 Not more than 10%, heating the gas-based shaft furnace top purified gas to 360 ℃ by using the convection section of the preheating furnace 3, mixing the gas-based shaft furnace top purified gas with the reducing gas at the temperature of 1100-1200 ℃ in the outlet pipeline 21 of the reforming furnace 2, and controlling the flow rate of the gas-based shaft furnace top purified gas to ensure that the temperature of the mixed reducing gas in the mixed reducing gas pipeline 7 is 850-1100 ℃.
The technical features not disclosed in the present embodiment are the same as those in the embodiment.
In the above embodiments, the preheating furnace 3 is an external combustion tube type heating furnace, the preheating furnace 3 may also be a coke oven dry quenching hot medium gas heat exchanger, a heat exchange furnace tube may also be inserted into a combustion chamber of the coke oven as a heat exchange tube of the preheating furnace 3, or a heat exchange furnace tube may be inserted into a refractory material on the top of the coke oven as a heat exchange tube of the preheating furnace 3.
The above-mentioned list is only the preferred embodiment of the present invention, and naturally those skilled in the art can make modifications and variations to the present invention, which should be considered as the protection scope of the present invention provided they are within the scope of the claims of the present invention and their equivalents.
Claims (10)
1. A method for preparing reducing gas of a gas-based shaft furnace by taking rich hydrocarbon gas as raw material gas comprises the steps of pressurizing the raw material gas, heating the raw material gas by a heating furnace to prepare the reducing gas required by the gas-based shaft furnace, and feeding the reducing gas into the gas-based shaft furnace from a tuyere of the gas-based shaft furnace, and is characterized in that: preheating the first hydrocarbon-rich gas to 250-700 ℃, then feeding the first hydrocarbon-rich gas into a non-catalytic partial oxidation converter, combusting the first hydrocarbon-rich gas with pure oxygen to perform partial oxidation reaction, controlling the combustion temperature to enable the temperature of reducing gas at an outlet of the converter to be 1100-1200 ℃, then mixing the second hydrocarbon-rich gas or purified gas decarbonized at the top of a gas-based shaft furnace into the reducing gas at an outlet pipeline of the converter to form mixed gas at the temperature of 850-1100 ℃, and feeding the mixed gas into the gas-based shaft furnace from a tuyere of the gas-based shaft furnace.
2. The method for preparing a gas-based shaft furnace reducing gas by using a hydrocarbon-rich gas as a raw material gas according to claim 1, wherein the method comprises the following steps: preheating the first hydrocarbon-rich gas to 250-350 ℃, then entering a non-catalytic partial oxidation converter, and combusting with pure oxygen.
3. The method according to claim 1, wherein the gas-based shaft furnace reducing gas is prepared from a hydrocarbon-rich gas as a raw material gas, and the method comprises the following steps: preheating the first hydrocarbon-rich gas to 500-700 ℃, and then feeding the first hydrocarbon-rich gas into a non-catalytic partial oxidation converter to be combusted with pure oxygen.
4. A method for producing a reducing gas for a gas-based shaft furnace using a hydrocarbon-rich gas as a raw material gas according to any one of claims 1 to 3, characterized in that: preheating the second hydrocarbon-rich gas to a certain temperature, and mixing the second hydrocarbon-rich gas into the reducing gas of the outlet pipeline of the reformer.
5. The method according to claim 2, wherein the gas-based shaft furnace reducing gas is a hydrocarbon-rich gas as a raw material gas, and the method comprises the following steps: and preheating the second hydrocarbon-rich gas to 250-350 ℃, and mixing the second hydrocarbon-rich gas into the reducing gas of the outlet pipeline of the reformer.
6. The method according to claim 5, wherein the gas-based shaft furnace reducing gas is prepared from a hydrocarbon-rich gas as a raw material gas, and the method comprises the following steps: the preheating temperature of the first hydrocarbon-rich gas and the second hydrocarbon-rich gas is 280-300 ℃.
7. The method according to claim 3, wherein the gas-based shaft furnace reducing gas is prepared from a hydrocarbon-rich gas as a raw material gas, and the method comprises the following steps: and preheating the second hydrocarbon-rich gas to 500-700 ℃, and mixing the second hydrocarbon-rich gas into the reducing gas of the outlet pipeline of the reformer.
8. The method for preparing a gas-based shaft furnace reducing gas by using a hydrocarbon-rich gas as a raw material gas according to claim 7, characterized in that: the preheating temperature of the first hydrocarbon-rich gas and the second hydrocarbon-rich gas is 600-700 ℃.
9. The method for producing a reducing gas for a gas-based shaft furnace using a hydrocarbon-rich gas as a raw material gas according to claims 1, 3, 7 and 8, wherein: when the first hydrocarbon-rich gas and the second hydrocarbon-rich gas are preheated to more than 500 ℃, unsaturated hydrocarbons in the hydrocarbon-rich gas need to be converted into saturated hydrocarbons.
10. The method according to claim 9, wherein the gas-based shaft furnace reducing gas is a hydrocarbon-rich gas as a raw material gas, and the method comprises the following steps: before preheating the first hydrocarbon-rich gas and the second hydrocarbon-rich gas, organic sulfur in the hydrocarbon-rich gas needs to be converted into H2S.
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| CN103525964B (en) * | 2013-10-08 | 2016-05-25 | 中国石油大学(北京) | Utilize oven gas catalyzed conversion to produce the method and system of gas base directly reducing iron |
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