CN218666128U - Hydrogen-based shaft furnace direct reduction device - Google Patents
Hydrogen-based shaft furnace direct reduction device Download PDFInfo
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- CN218666128U CN218666128U CN202122826644.4U CN202122826644U CN218666128U CN 218666128 U CN218666128 U CN 218666128U CN 202122826644 U CN202122826644 U CN 202122826644U CN 218666128 U CN218666128 U CN 218666128U
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- 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
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- Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
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Abstract
The utility model discloses a hydrogen base shaft furnace direct reduction device belongs to in the direct reduction field. The reduction gas pipeline is communicated with an inlet of the gas heating device, an outlet of the gas heating device is communicated with a reduction section air port of the shaft furnace body, the reduction gas pipeline is a hydrocarbon-rich gas pipeline, an inner cavity of the gas heating device is only provided with one cavity, a lining of the gas heating device is made of refractory materials, and an outlet pipeline of the gas heating device is communicated with any one of the following structures: (1) After being connected in parallel with the unheated hydrocarbon-rich gas pipeline, the furnace body is communicated with a tuyere at the reduction section of the shaft furnace body; (2) The outlet of the heat exchanger is communicated with the air port of the reduction section of the shaft furnace body; (3) And H 2 And one of COOr after the pipelines of the two gas mixtures are connected in parallel, the pipelines are communicated with the tuyere at the reduction section of the shaft furnace body. The utility model has low overall investment, the heating furnace adopts the refractory material lining, and the reaction can be carried out when the temperature is higher than 1100 ℃, so that CH 4 The conversion rate is high, and the risk of carbon deposition is reduced.
Description
Technical Field
The utility model belongs to the direct reduction field, concretely relates to hydrogen base shaft furnace direct reduction device.
Background
The prior art of gas-based shaft furnace direct reduction, for example, patent application No. 201210379144.3, entitled direct reduction process for producing sponge iron by using rich CH4 coal gas, proposes "adjusting the pressure of the rich CH4 coalInputting gas and gas-based shaft furnace top gas subjected to temperature reduction, dust removal and pressurization treatment in sequence into an external converter, and supplementing steam serving as a CH4 modifying reaction oxidant into the external converter, so that CH4, H2O and CO2 in the external converter are subjected to modifying reaction under the action of a catalyst to generate high-temperature reducing gas mainly comprising CO and H2, wherein the temperature of the reducing gas at the outlet of the converter is 850 ℃; for another example, patent No. 201710676084.4, entitled "system and method for preparing gas-based shaft furnace reducing gas," the system for preparing gas-based shaft furnace reducing gas includes a gas-based shaft furnace top gas scrubber, a top gas decarbonization device, a coke oven gas purification device, a coke oven gas desulfurization device, a reformer, a heat recovery device, a synthesis gas dust removal device, a synthesis gas desulfurization and decarbonization device, and a mixer, "the catalyst tubes are arranged in parallel, the heat recovery device is a heat exchanger," in the catalytic reforming reaction of the present invention, CH4, CO2 in the coke oven gas and CO2 in the top gas are reformed as raw materials into high temperature shift gas rich in CO and H2 at a temperature of 800-1000 ℃; for another example, application No.: CN201910952204.8, entitled "reforming furnace for producing reducing gas," which comprises a radiant chamber box, a reforming furnace tube, a burner, a transition section and a convection section; the reforming furnace tubes are arranged in 2m rows and are vertically arranged in the radiation chamber box body in parallel; one row of reforming furnace tubes corresponds to one reforming raw material gas inlet branch main tube, each reforming raw material gas inlet branch main tube is provided with branches with the same number as that of each row of reforming furnace tubes, and the gas inlets of the reforming furnace tubes are connected with the reforming raw material gas inlet branch main tubes through flexible tubes; the burners (2m + 1) are arranged on the bottom wall plate below the radiation chamber; the gas outlet of the reforming furnace tube is connected with the cold wall branch pipe through an inclined tee; the transition section is that a plurality of transition section branch pipes are arranged above two side wall plates of the radiation chamber box body and led out to a transition section branch main pipe, and the two transition section branch main pipes are converged into a transition section main pipe at one end of the radiation chamber box body; the transition section header pipe is connected with the convection section, and the convection section is connected with the chimney through the induced draft fan; the convection section consists of more than or equal to 4 heat exchangers, and the heat exchangers are a flash evaporator, a reforming raw material preheater, a steam superheater and a de-dredging coke oven gas preheaterAt least 4 of a heat exchanger, a top gas preheater and a combustion air preheater; the high temperature reformed gas product at 910 ℃ is sent to a shaft furnace for the next stage reaction ". The three prior art patents are that hydrocarbon-rich gas (such as natural gas and coke oven gas) and top gas of a shaft furnace are mixed and heated in a tubular converter, and the mixed gas is injected into the shaft furnace after being heated to 850-1000 ℃. Such a process has the following problems: (1) Because the reforming tubes are externally heated, the diameter of the reforming tubes is limited, and the volume of a single reforming tube is small and the number of the reforming tubes is large. The number of reforming tubes is as many as several hundred, and the number of burners is several tens. This results in a large and complex installation of the radiant chamber heating system equipment; (2) The high temperature resistant reforming tubes and burners are very expensive, and a set of reforming furnace equipment usually requires hundreds of reforming tubes, thus the investment is too large; (3) Because the material of the high-temperature resistant furnace tube is limited, the gas heating temperature cannot exceed 1000 ℃, so that the conversion rate of hydrocarbon under the condition of no catalyst is limited; (4) The transition section and convection section equipment for discharging flue gas and utilizing flue gas waste heat are huge, the structure is complex, and the investment cost is increased again: (5) The CH 4-rich gas and the non-hydrocarbon top gas are mixed to participate in CH 1 The reforming of (2) increases the volume of the reformer and the amount of catalyst.
As yet another example, patent application No. CN201280070307.8, entitled Direct Reduced Iron (DRI) production using coke oven gas, proposes "providing a gas heater design that minimizes carbon deposits when heating COG or similar syngas, or providing on-line cleaning measures to remove carbon deposits periodically to avoid fouling and plugging the heater tubes. ", which is essentially carried out by using as a first reducing gas stream a mixed gas of hydrogen and carbon monoxide containing no hydrocarbons and as a second stream a gas containing coke oven gas, heating the first stream and then mixing the second stream into the first stream so that the resulting mixture forms a third gas stream at a temperature above 700 ℃, thereby minimizing said carbon deposits from the carbon compounds present in the second stream comprising COG. The problems of this solution are: (1) The scheme adopts external heat, is limited by the heat resistance of a pipe, has the highest temperature not exceeding 980 ℃, namely the third gas flow in the patent is between 700 and 980 ℃, and is closer to 700 ℃ in order to add the gas amount into a coke oven, and the reaction of reforming the hydrocarbon into H2 and CO starts at the temperature of above 700 ℃, so that the conversion rate of reforming the hydrocarbon into H2 and CO is limited in the temperature range, the lower the conversion rate of the hydrocarbon is, the larger the carbon deposition amount is, the problem of carbon deposition is solved in a limited manner, and the problem of carbon deposition cannot be solved; (2) When carbon deposition is cleaned, the pipeline is complex, a plurality of high-temperature valves are arranged, and the implementation is difficult in practical application.
Disclosure of Invention
In order to solve the technical problem, the utility model provides a gas-based shaft furnace direct reduction device.
One of the purposes of the utility model is to reduce the overall investment of the project.
The second purpose of the utility model is to simplify the structure of the gas heating device.
The third purpose of the utility model is to improve the utilization rate of the raw material gas.
The fourth purpose of the utility model is to improve the conversion rate of hydrocarbon-rich gas and reduce the risk of carbon deposition.
Other objects of the invention will be pointed out hereinafter or will be apparent to those skilled in the art.
In order to achieve the purpose, the utility model discloses reduction device adopts following technical scheme:
the utility model provides a hydrogen base shaft furnace direct reduction device, including shaft furnace device and gas heating device, the shaft furnace device includes charging devices, the shaft furnace body, discharging device, shaft furnace top coal gas purifier, the shaft furnace body includes preheating section, reduction section and cooling zone, the reduction gas pipeline communicates with gas heating device import, the gas heating device export communicates with shaft furnace body reduction section wind gap, wherein the reduction gas pipeline is rich hydrocarbon gas pipeline, the gas heating device inner chamber only has a cavity, the gas heating device inside lining is refractory material, gas heating device export pipeline communicates with following arbitrary kind of structure:
(1) After being connected in parallel with the unheated hydrocarbon-rich gas pipeline, the furnace body is communicated with a tuyere at the reduction section of the shaft furnace body;
(2) The outlet of the heat exchanger is communicated with the air port of the reduction section of the shaft furnace body;
(3) And H 2 And one gas or a mixture of two gases in the CO are connected in parallel and then are communicated with a tuyere of a reduction section of the shaft furnace body.
Compared with the prior art, the utility model discloses following beneficial effect has:
(1) And (3) reducing the overall investment of the project: a, a heating furnace with a refractory material lining is used for replacing a heating furnace consisting of hundreds of heat-resistant steel pipes, so that the investment is reduced; b, no catalyst is used, so that the requirement on the sulfur content of the hydrocarbon-rich gas is lowered, the working procedure is simplified, and the investment is reduced; and c, no complex and huge heat exchange system is provided, so that the investment is further reduced.
(2) The utilization rate of the raw material gas is improved: mixing with H in the hydrocarbon-rich gas 2 And/or a hydrocarbon-rich gas CH alone, after CO reaction, in comparison with oxygen 1 Higher content, and when reacting with oxygen to generate high temperature gas, generating effective gas H 2 The amount of + CO is larger, which improves the utilization rate of the raw material gas and reduces the energy consumption at the same time. And mix into H 2 And/or CO, to reach high temperatures, H is increased 2 And consumption of CO to produce an ineffective component H 2 O or CO 2 。
(3) Since the furnace is lined with refractory material, the hydrocarbon-rich gas and the oxidant can react at temperatures above 1100 ℃, CH 1 The conversion rate is high, reduces the carbon deposit risk, the utility model discloses a heating furnace of refractory material inside lining can satisfy the requirement of high temperature more than 1100 ℃.
(4) The gas heating furnace has a simple structure and only has one cavity, and the traditional tubular heating furnace consists of hundreds of steel tube cavities.
(5) Without a bulky heat exchange system.
The utility model discloses an optimal scheme does:
after the outlet pipeline of the gas heating device is connected with the unheated hydrocarbon-rich gas pipeline in parallel, the following scheme is further adopted:
(1) The outlet pipeline of the gas heating device is connected with the unheated hydrocarbon-rich gas pipeline in parallel and then connected with the H 2 Is connected with a pipeline of one gas or a mixture of two gases in the CO in parallel to form a main pipeline which is communicated with a tuyere at the reduction section of the shaft furnace body
(2) The outlet pipeline of the gas heating device and the pipeline after the unheated hydrocarbon-rich reducing gas is connected in parallel are communicated with a row of air doors of the reduction section of the shaft furnace body, and heated H 2 And a pipeline of one gas or a mixture of two gases in the CO is communicated with the other air exhaust port of the reduction section of the shaft furnace body.
After the outlet pipeline of the gas heating device is communicated with the inlet of the heat exchanger, the following scheme is further adopted:
(1) Heat exchanger outlet pipe and H 2 And one gas or a mixture of two gases in the CO is communicated with a pipeline and then is communicated with a tuyere of a reduction section of the shaft furnace body.
(2) An outlet pipeline of the heat exchanger, which is communicated with an exhaust port of the reduction section of the shaft furnace body and is heated by the heated H 2 And a pipeline of one gas or a mixture of two gases in the CO is communicated with the other air exhaust port of the reduction section of the shaft furnace body.
Furthermore, the outlet pipeline of the gas heating device is connected with the pipeline after the unheated hydrocarbon-rich gas pipeline is connected in parallel, and then is connected with the H 2 The pipeline which is connected with one gas or the mixture of two gases in the CO is connected in parallel, the pipeline which is connected in parallel is communicated with an exhaust port of the reduction section of the shaft furnace body, and the heated H 2 And a pipeline of one gas or a mixture of two gases in the CO is communicated with the other air outlet of the reduction section of the shaft furnace body.
Further, the heat exchanger outlet pipeline is connected with the H 2 The heated H is communicated with a blast hole of a reduction section of the shaft furnace body after being communicated with a pipeline of one gas or a mixture of two gases in the CO 2 And a pipeline of one gas or a mixture of two gases in the CO is communicated with an exhaust port of the reduction section of the shaft furnace body.
In the scheme, the hydrocarbon-rich gas adopts a heating device of a partial oxidation conversion furnace.
When two air outlets are arranged on the reduction section of the shaft furnace body, the upper air outlet and the lower air outlet are arranged in a staggered manner, namely the upper air outlet and the lower air outlet are not on the same vertical line.
Furthermore, each air outlet of the upper row is positioned on a vertical bisector of a horizontal arc line which is formed by connecting two adjacent air outlets of the lower row.
Drawings
FIG. 1 is a drawing of a direct reduction apparatus of a hydrogen-based shaft furnace according to the present invention;
FIG. 2 is a diagram of a second hydrogen-based shaft furnace direct reduction apparatus of the present invention;
FIG. 3 is a diagram of a third hydrogen-based shaft furnace direct reduction apparatus of the present invention;
FIG. 4 is a drawing of a fourth hydrogen-based shaft furnace direct reduction apparatus of the present invention;
FIG. 5 is a drawing of a fifth hydrogen-based shaft furnace direct reduction apparatus of the present invention;
FIG. 6 is a drawing of a sixth hydrogen-based shaft furnace direct reduction apparatus of the present invention;
FIG. 7 is a diagram of a seventh hydrogen-based shaft furnace direct reduction apparatus of the present invention;
FIG. 8 is a drawing of an eighth hydrogen-based shaft furnace direct reduction apparatus according to the present invention;
FIG. 9 is a drawing of a ninth hydrogen-based shaft furnace direct reduction apparatus of the present invention;
fig. 10 is a schematic view of the tuyere arrangement on the hydrogen-based shaft furnace of the present invention.
Labeled as: 1-gas-based shaft furnace, 2-partial oxidation reforming furnace, 3-burner, 4-oxygen, 5-hydrocarbon-rich gas main pipe, 6-gas pipe at top of shaft furnace, 7-steam main pipe and 8-H 2 And/or heating means for CO, 9-heat exchanger, 11-preheating section of shaft furnace, 12-reducing section of shaft furnace, 13-cooling section of shaft furnace, 14-charging means, 15-tuyere of shaft furnace, 16-discharging means, 21-outlet pipeline of reforming furnace, 51-first branch of hydrocarbon-rich gas, 52-second branch of hydrocarbon-rich gas, 61-dust remover, 62-decarbonating means, 71-water pipe, 151-first tuyere of shaft furnace, 152-second tuyere of shaft furnace, a 1-first tuyere of first row, a 2-second tuyere of first row, a 3-third tuyere of first row, a 4-fourth tuyere of first row, a 5-fifth tuyere of first row, b 1-first tuyere of second row, b 2-second tuyere of second row, b 3-third tuyere of second row, b 4-fourth tuyere of second row, b 5-fifth tuyere of second row.
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 functions of the present invention, but the present invention is not limited thereto.
Please refer to fig. 1. The hydrogen-based shaft furnace direct reduction device comprises a gas-based shaft furnace 1 and a partial oxidation reforming furnace 2, wherein the gas-based shaft furnace 1 comprises a charging device 14, a discharging device 16, a shaft furnace preheating section 11, a shaft furnace reduction section 12 and a cooling section 13, a hydrocarbon-rich gas main pipe 5 is divided into two pipelines, namely a hydrocarbon-rich gas first branch pipe 51 and a hydrocarbon-rich gas second branch pipe 52, the hydrocarbon-rich gas branch pipe 51 is communicated with a hydrocarbon-rich gas inlet of a burner 3 in the partial oxidation reforming furnace 2, oxygen 4 enters an oxygen inlet of the burner 3, the hydrocarbon-rich gas and the oxygen enter the partial oxidation reforming furnace 2 through the burner 3 for combustion, and the gas after combustion and heating enters an outlet pipeline 21 of the partial oxidation reforming furnace 2. The hydrocarbon-rich gas branch pipe 52 is connected with the outlet pipeline 21 of the partial oxidation reformer 2 in parallel and then communicated with the tuyere 15 of the reduction section of the shaft furnace. The top gas generated by the reaction is discharged from a top gas pipe 6 of the shaft furnace and is sent to a coke oven, a blast furnace hot blast stove or a steel rolling heating furnace to be used as a heating fuel. The steam is introduced into the burner 3 of the reformer 2 through a steam manifold 7. The method can be used for facilitating the reforming of methane in the hydrocarbon-rich gas into H 2 And CO, and the furnace top of the converter 2 and the burner 3 can be protected by reducing the temperature through the steam.
Please refer to fig. 2. The hydrogen-based shaft furnace direct reduction device comprises a gas-based shaft furnace 1 and a partial oxidation converter 2, wherein the gas-based shaft furnace 1 comprises a charging device 14, a discharging device 16, a shaft furnace preheating section 11, a shaft furnace reduction section 12 and a cooling section 13. The hydrocarbon-rich gas main pipe 5 is communicated with a hydrocarbon-rich gas inlet of a burner 3 in the partial oxidation reformer 2, oxygen 4 enters an oxygen inlet of the burner 3, the hydrocarbon-rich gas and the oxygen enter the partial oxidation reformer 2 through the burner 3 for combustion, and the gas after combustion and heating enters an outlet pipeline 21 of the partial oxidation reformer 2. An outlet pipeline 21 of the partial oxidation reforming furnace 2 is communicated with an inlet of a reducing gas pipeline in the heat exchanger 9, and an outlet of the reducing gas pipeline in the heat exchanger 9 is communicated with a tuyere 15 of a reduction section of the shaft furnace. The water pipe 71 is communicated with the inlet of the box body of the heat exchanger 9, and the outlet of the box body of the heat exchanger 9 is communicated with the steam inlet of the burner 3 of the reformer 2 through the steam main pipe 7. The top gas generated by the reaction is discharged from a top gas pipe 6 of the shaft furnace and is sent to a coke oven, a blast furnace hot blast stove or a steel rolling heating furnace to be used as a heating fuel.
Please refer to fig. 3. The hydrogen-based shaft furnace direct reduction device comprises a gas-based shaft furnace 1 and a partial oxidation converter 2, wherein the gas-based shaft furnace 1 comprises a charging device 14, a discharging device 16, a shaft furnace preheating section 11, a shaft furnace reduction section 12 and a cooling section 13. The hydrocarbon-rich gas main pipe 5 is communicated with a hydrocarbon-rich gas inlet of a burner 3 in the partial oxidation reforming furnace 2, oxygen 4 enters an oxygen inlet of the burner 3, the hydrocarbon-rich gas and the oxygen enter the partial oxidation reforming furnace 2 through the burner 3 for combustion, and the gas after combustion and heating enters an outlet pipeline 21 of the partial oxidation reforming furnace 2. The outlet pipeline 21 of the partial oxidation reformer 2 is connected with the top gas pipeline 6 passing through the dust remover 61 and the carbon dioxide removal device 62 in parallel and then is communicated with the tuyere 15 of the reduction section of the shaft furnace. The steam is introduced into the burners 3 of the reformer 2 through a steam header 7. The method can help to reform methane in the hydrocarbon-rich gas into H 2 And CO, and the furnace top and the burner 3 of the reformer 2 can be protected by cooling through the steam. The main component of the top gas after passing through the dust remover 61 and the carbon dioxide removal device 62 is H 2 And CO.
Please refer to fig. 4. The hydrogen-based shaft furnace direct reduction device comprises a gas-based shaft furnace 1 and a partial oxidation converter 2, wherein the gas-based shaft furnace 1 comprises a charging device 14, a discharging device 16, a shaft furnace preheating section 11, a shaft furnace reduction section 12 and a cooling section 13. The hydrocarbon-rich gas main pipe 5 is divided into two pipelines, namely a hydrocarbon-rich gas first branch pipe 51 and a hydrocarbon-rich gas second branch pipe 52, wherein the hydrocarbon-rich gas first branch pipe 51 is communicated with a hydrocarbon-rich gas inlet of a burner 3 in the partial oxidation reforming furnace 2, oxygen 4 enters an oxygen inlet of the burner 3, the hydrocarbon-rich gas and the oxygen enter the partial oxidation reforming furnace 2 through the burner 3 for combustion, and the gas after combustion and heating enters an outlet pipeline 21 of the partial oxidation reforming furnace 2. The hydrocarbon-rich gas branch pipe 52 is connected in parallel with the outlet pipeline 21 of the partial oxidation reformer 2, then connected in parallel with the top gas pipeline 6 passing through the dust remover 61 and the decarbonizing device 62, and then communicated with the tuyere 15 of the reduction section of the shaft furnace. The steam is introduced into the burner 3 of the reformer 2 through a steam manifold 7. The method can help to reform methane in the hydrocarbon-rich gas into H 2 And CO, and the furnace top and the burner 3 of the reformer 2 can be protected by cooling through the steam. The main component of the top gas after passing through the dust remover 61 and the carbon dioxide removal device 62 is H 2 And CO.
Please refer to fig. 5. The hydrogen-based shaft furnace direct reduction device comprises a gas-based shaft furnace 1 and a partial oxidation converter 2, wherein the gas-based shaft furnace 1 comprises a charging device 14, a discharging device 16, a shaft furnace preheating section 11, a shaft furnace reduction section 12 and a cooling section 13. The hydrocarbon-rich gas main pipe 5 is communicated with a hydrocarbon-rich gas inlet of a burner 3 in the partial oxidation reformer 2, oxygen 4 enters an oxygen inlet of the burner 3, the hydrocarbon-rich gas and the oxygen enter the partial oxidation reformer 2 through the burner 3 for combustion, and the gas after combustion and heating enters an outlet pipeline 21 of the partial oxidation reformer 2. The outlet pipeline 21 of the partial oxidation reforming furnace 2 is communicated with the inlet of a reducing gas pipeline in the heat exchanger 9, and the outlet of the reducing gas pipeline in the heat exchanger 9 is connected with a furnace top gas pipeline 6 which passes through a dust remover 61 and a carbon dioxide removal device 62 in parallel and then communicated with a tuyere 15 of a reduction section of the shaft furnace. The water pipe 71 is communicated with the inlet of the box body of the heat exchanger 9, and the outlet of the box body of the heat exchanger 9 is communicated with the steam inlet of the burner 3 of the reformer 2 through the steam main pipe 7. The main component of the top gas after passing through the dust remover 61 and the carbon dioxide removal device 62 is H 2 And CO.
Please refer to fig. 6. The hydrogen-based shaft furnace direct reduction device comprises a gas-based shaft furnace 1 and a partial oxidation converter 2, wherein the gas-based shaft furnace 1 comprises a charging device 14, a discharging device 16, a shaft furnace preheating section 11, a shaft furnace reduction section 12 and a cooling section 13. The hydrocarbon-rich gas main pipe 5 is divided into two pipelines which are a hydrocarbon-rich gas first branch pipe 51 and a hydrocarbon-rich gas second branch pipe 52 respectively, wherein the hydrocarbon-rich gas branch pipe 51 is communicated with a hydrocarbon-rich gas inlet of a burner 3 in the partial oxidation reformer 2, oxygen 4 enters an oxygen inlet of the burner 3, the hydrocarbon-rich gas and the oxygen enter the partial oxidation reformer 2 through the burner 3 for combustion, and the gas after combustion and heating enters an outlet pipeline 21 of the partial oxidation reformer 2. The hydrocarbon-rich gas branch pipe 52 is connected with the outlet pipeline 21 of the partial oxidation converter 2 in parallel and then communicated with the tuyere 152 of the reduction section of the shaft furnace. The top gas pipeline 6 after passing through the dust remover 61 and the carbon dioxide removal device 62 is communicated with the inlet of the heating device 8, and the outlet of the heating device 8 is communicated with the tuyere 151 of the reduction section of the shaft furnace. The steam is introduced into the burners 3 of the reformer 2 through a steam header 7. The method can help to reform methane in the hydrocarbon-rich gas into H 2 And CO, and the furnace top and the burner 3 of the reformer 2 can be protected by cooling through the steam.The arrangement of the two air outlets increases the operation and adjustment means of the gas-based shaft furnace, and improves the product quality.
Please refer to fig. 7. The hydrogen-based shaft furnace direct reduction device comprises a gas-based shaft furnace 1 and a partial oxidation reforming furnace 2, wherein the gas-based shaft furnace 1 comprises a charging device 14, a discharging device 16, a shaft furnace preheating section 11, a shaft furnace reduction section 12 and a cooling section 13 rich hydrocarbon gas main pipe 5 which is communicated with a rich hydrocarbon gas inlet of a burner 3 in the partial oxidation reforming furnace 2, oxygen 4 enters an oxygen inlet of the burner 3, rich hydrocarbon gas and oxygen enter the partial oxidation reforming furnace 2 through the burner 3 for combustion, and gas after combustion and heating enters an outlet pipeline 21 of the partial oxidation reforming furnace 2. The outlet pipeline 21 of the partial oxidation reforming furnace 2 is communicated with the inlet of a reducing gas pipeline in the heat exchanger 9, and the outlet of the reducing gas pipeline in the heat exchanger 9 is communicated with a tuyere 152 of a reduction section of the shaft furnace. The furnace top gas pipeline 6 after passing through the dust remover 61 and the carbon dioxide removal device 62 is communicated with the inlet of a heating device 8, the outlet of the heating device 8 is communicated with a blast hole 151 of a reduction section of the shaft furnace, a water pipe 71 is communicated with the inlet of a box body of a heat exchanger 9, and the outlet of the box body of the heat exchanger 9 is communicated with the steam inlet of a burner 3 of the reformer 2 through a steam main pipe 7. The main component of the top gas after passing through the dust remover 61 and the carbon dioxide removal device 62 is H 2 And CO.
Please refer to fig. 8. Fig. 8 differs from the apparatus of fig. 6 in that the top gas line 6, which has passed through the dust separator 61 and the decarbonation apparatus 62, is branched into two branch lines: one branch pipeline is communicated with an inlet of the heating device 8, and an outlet of the heating device 8 is communicated with a tuyere 151 of a reduction section of the shaft furnace; the parallel connection of the hydrocarbon-rich gas branch pipe 52 and the reformer outlet pipe 21 is connected with another branch pipe in parallel, and then is communicated with the shaft furnace reduction section tuyere 152.
Please refer to fig. 9. Fig. 9 differs from the apparatus of fig. 7 in that the top gas line 6, after passing through the dust separator 61 and the decarbonation apparatus 62, is divided into two branch lines: one branch pipeline is communicated with an inlet of the heating device 8, and an outlet of the heating device 8 is communicated with a tuyere 151 of a reduction section of the shaft furnace; the other branch pipeline is connected in parallel with the outlet pipeline of the reducing gas pipeline in the heat exchanger 9 and then communicated with the tuyere 152 of the reduction section of the shaft furnace.
Please refer to fig. 10. Fig. 10 is a front view of the gas-based shaft furnace and a schematic view of the tuyere arrangement on the gas-based shaft furnace. Two air outlets are arranged on the reduction section of the gas-based shaft furnace, and each air outlet is uniformly distributed around the reduction section of the gas-based shaft furnace, namely a1, a2, a3, a4 and a5. The problem of uneven distribution of airflow and temperature on the cross section of the gas-based shaft furnace is solved. For example, the tuyere a1 is added vertically above the tuyere b1 and the tuyere b2, so that the problems of weak airflow and low temperature between the tuyere b1 and the tuyere b2 are solved. The diameter of the upper air outlet and the diameter of the lower air outlet can be adjusted to achieve the purpose that the upper air outlet blows to the center of the air permeable base shaft furnace and the lower air outlet blows to the periphery of the air permeable base shaft furnace. The upper and lower air outlets can be interchanged, namely the lower air outlet blows to the center of the air-permeable base shaft furnace, and the upper air outlet blows to the periphery of the air-permeable base shaft furnace. The arrangement of the two air outlets increases the operation and adjustment means of the gas-based shaft furnace, and improves the product quality.
The preferred embodiments of the present invention have been shown and described, and it will be understood that modifications and variations may be made by those skilled in the art without departing from the scope of the invention.
Claims (10)
1. The utility model provides a hydrogen base shaft furnace direct reduction device, including shaft furnace device and gas heating device, the shaft furnace device includes charging devices, the shaft furnace body, discharging device, shaft furnace top coal gas purifier, the shaft furnace body includes preheating section, reduction section and cooling zone, the reduction gas pipeline communicates with the gas heating device import, the gas heating device export communicates with shaft furnace body reduction section wind gap, its characterized in that reduction gas pipeline is rich hydrocarbon gas pipeline, gas heating device's inner chamber only has a cavity, the gas heating device inside lining is refractory material, gas heating device export pipeline communicates with following arbitrary kind of structure:
(1) After being connected in parallel with a branch pipeline of the hydrocarbon-rich gas pipeline, the gas pipeline is communicated with a tuyere at the reduction section of the shaft furnace body;
(2) The outlet of the heat exchanger is communicated with an air port of a reduction section of the shaft furnace body;
(3) Is connected in parallel with a furnace top gas pipeline passing through the dust remover and the carbon dioxide removal device and then is communicated with a tuyere at the reduction section of the shaft furnace body.
2. The direct reduction device of claim 1, wherein an outlet pipeline of the gas heating device is connected in parallel with a branch pipeline of the hydrocarbon-rich gas pipeline and then connected in parallel with a top gas pipeline passing through the dust remover and the carbon dioxide removal device to form a main pipeline, and the main pipeline is further communicated with an air port of a reduction section of the shaft furnace body.
3. The direct reduction device of the hydrogen-based shaft furnace according to claim 1, wherein an outlet pipeline of the gas heating device is communicated with an inlet of a heat exchanger, and an outlet of the heat exchanger is communicated with a tuyere of a reduction section of a shaft furnace body after being connected in parallel with a top gas pipeline after passing through a dust remover and a carbon dioxide removal device.
4. The direct reduction device of claim 1, wherein the outlet pipeline of the gas heating device and the branch pipeline of the hydrocarbon-rich gas pipeline are connected in parallel, and are communicated with an exhaust port of the reduction section of the shaft furnace body, the top gas pipeline after passing through the dust remover and the decarbonation device is communicated with one inlet of the heating device, and one outlet of the heating device is communicated with the other exhaust port of the reduction section of the shaft furnace body.
5. The direct reduction device of the hydrogen-based shaft furnace according to claim 1, wherein an outlet pipeline of the heat exchanger is communicated with an exhaust port of the reduction section of the shaft furnace body, a top gas pipeline after the dust remover and the carbon dioxide removal device is communicated with an inlet of the heating device, and an outlet of the heating device is communicated with another exhaust port of the reduction section of the shaft furnace body.
6. The direct reduction device of the hydrogen-based shaft furnace according to claim 4, wherein the top gas pipeline after the dust remover and the decarbonation device is divided into two branch pipelines: one branch pipeline is communicated with an inlet of a heating device, and an outlet of the heating device is communicated with an exhaust port of a reduction section of the shaft furnace; the branch pipeline of the hydrocarbon-rich gas pipeline is connected with the outlet pipeline of the gas heating device in parallel, then is connected with another branch pipeline of the furnace top gas in parallel, and then is communicated with another air outlet of the reduction section of the shaft furnace.
7. The direct reduction device of claim 5, wherein the top gas pipeline after the dust remover and the decarbonation device is divided into two branch pipelines: one branch pipeline is communicated with an inlet of a heating device, and an outlet of the heating device is communicated with an exhaust port of the reduction section of the shaft furnace; the other branch pipeline is connected with the outlet pipeline of the reducing gas pipeline in the heat exchanger in parallel and then communicated with the other air exhaust port of the reduction section of the shaft furnace.
8. A hydrogen-based shaft furnace direct reduction plant according to any of claims 1 to 7, characterized in that the hydrocarbon-rich gas employs a partial oxidation reformer heating means.
9. A hydrogen-based shaft furnace direct reduction device according to any one of claims 4 to 7, characterized in that the upper tuyere and the lower tuyere of the reduction section of the shaft furnace body are arranged in a staggered manner, i.e. the upper tuyere and the lower tuyere are not on a vertical line.
10. The direct reduction device of claim 9, wherein each of the upper row of tuyeres is located on a vertical bisector of a horizontal arc connecting two tuyeres of the adjacent lower row.
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