Method for calcining cement clinker under hydrogen- and oxygen-enriched conditions

Abstract

Disclosed in the present invention is a method for calcining cement clinker under hydrogen- and oxygen-enriched conditions. In the method, oxygen-enriched combustion is used at a kiln head of a rotary kiln, the oxygen-enriched combustion is realized by a first energy supply unit and an oxygen supply unit, and the oxygen supply unit delivers oxygen into a third pipe and a fourth pipe by means of a first branch and a second branch to increase the oxygen content of conveyed air, thereby realizing oxygen-enriched combustion at the kiln head. Hydrogen-enriched combustion is used in a decomposition furnace, the hydrogen-enriched combustion is realized by a hydrogen supply unit, and the hydrogen supply unit supplies hydrogen as a final combustion agent into the decomposition furnace at a kiln tail to realize hydrogen-enriched combustion. The present invention can increase the temperature of the flame at the kiln head, promotes burnout of fuel at the kiln head and kiln tail, improves energy utilization efficiency, decreases the resistance of a system, reduces heat consumption and power consumption, achieves carbon emission reduction in the cement industry, and has good economic and social benefits.

Description

A method for calcining cement clinker using hydrogen-rich and oxygen-rich methods Technical Field

[0001] This invention relates to the field of carbon emission reduction in the cement industry, and in particular to a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods. Background Technology

[0002] As global warming worsens, carbon dioxide emissions, as a greenhouse gas, have garnered widespread attention. In 2022, China's cement production reached 2.12 billion tons, with carbon emissions of 1.343 billion tons, accounting for 13% of China's total carbon emissions. The cement industry is the third largest carbon-emitting sector after electricity and steel. Achieving carbon neutrality remains a challenging journey. In 2022, the cement industry consumed approximately 200 million tons of coal, representing 4.05% of the national coal consumption. China's energy resources are characterized by "abundant coal, plentiful oil, and limited gas." During economic development, high-quality coal has been primarily utilized, leaving a large amount of low-quality coal unexploited. Improving the utilization of this low-quality coal and enriching the national energy structure is a hot research topic for many researchers.

[0003] To ensure stable calcination of cement clinker, cement plants primarily use high-quality coal fuels with low moisture content and high calorific value during production. Oxygen-enriched combustion, as a combustion technology, can improve fuel combustion conditions. Hydrogen, with its high calorific value and fast combustion speed, is an excellent clean fuel. Chinese Patent Publication No. CN111288792A discloses a partial oxygen-enriched calcination device for a cement rotary kiln, which can increase flame temperature and reduce coal usage, but it only reduces coal at the kiln head, neglecting the area at the kiln tail where coal usage is high. Chinese Patent Publication No. CN220153235U discloses an oxygen-enriched combustion system and cement calcination equipment for cement kilns, which can increase the application rate of alternative fuels, but the substitution rate is not high. Chinese Patent Publication No. CN113864776A discloses a method for carbon neutralization fuel substitution in the building materials industry, which requires various additives to adjust the hydrogen combustion flame, making the operation relatively complex. Chinese patent publication number CN115477484A discloses a zero-carbon emission cement production equipment and process using renewable hydrogen energy and pure oxygen combustion, but it uses all hydrogen as a substitute, which is less economical.

[0004] Therefore, there is an urgent need to develop a method for calcining cement clinker that can use only low-quality fuels (low-quality coal, alternative fuels, etc.) to enrich the energy structure, with a simple process, promote carbon emission reduction, and be economically viable.

[0005] Summary of the Invention

[0006] To address the problems existing in the prior art, this invention provides a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods. By combining kiln head oxygen-rich technology with kiln tail hydrogen-rich technology, this invention improves the utilization rate of low-quality fuels, including low-calorific-value coal and low-calorific-value alternative fuels. This ensures the intensity of the kiln head flame and the heat supply at the kiln tail, improves energy utilization efficiency, reduces carbon dioxide emissions, and provides a solution for the green and low-carbon development of the cement industry and the ultimate realization of carbon neutrality.

[0007] This invention is implemented as follows: a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods, comprising the following steps:

[0008] The raw materials are preheated in the preheating unit (1);

[0009] The preheated raw material is decomposed in the decomposition furnace (2);

[0010] The raw materials after calcination and decomposition in the rotary kiln (4);

[0011] The calcined cement clinker is cooled in the cooler (7);

[0012] Oxygen-enriched combustion is adopted at the kiln head of the rotary kiln (4). The oxygen-enriched combustion method is realized by the first energy supply unit and the oxygen supply unit (13). The first energy supply unit includes a fuel storage device (9), a feed scale (10), a fuel blower (11), and a primary air blower (12). The fuel storage device (9), the feed scale (10), and the fuel air inlet (501) of the kiln head burner (5) are connected in sequence. The fuel blower (11) is connected to the feed scale through the third pipeline (1603). The primary air fan (12) is connected to the axial primary air interface (502) and swirl primary air interface (503) of the kiln head burner (5) via the fourth pipeline (1604); the oxygen supply unit (13) is connected to the third pipeline (1603) via the first branch (1601) to increase the oxygen concentration in the fuel supply air; the oxygen supply unit (13) is connected to the fourth pipeline (1604) via the second branch (1602) to increase the oxygen concentration in the primary air.

[0013] Hydrogen-rich combustion is adopted in the decomposition furnace (2). The decomposition furnace (2) is equipped with a hydrogen burner (201), a decomposition furnace burner (202), and a tertiary air duct inlet (203). The hydrogen burner (201) is located above the tertiary air duct inlet (203). The hydrogen-rich combustion mode is realized by the hydrogen supply unit (14), which is connected to the hydrogen burner (201) and supplies hydrogen to the decomposition furnace (2) through the hydrogen burner (201) on the decomposition furnace (2).

[0014] The second power supply unit (15) is connected to the decomposition furnace burner (202) and supplies power to the decomposition furnace (2) through the decomposition furnace burner (202) on the decomposition furnace (2).

[0015] Furthermore, the fuel storage device (9) provides fuel with a calorific value of not less than 3500 kcal / kg and a moisture content of not more than 5%.

[0016] Furthermore, the second power supply unit (15) provides fuel with a calorific value of not less than 2000 kcal / kg and a moisture content of not more than 30%.

[0017] Furthermore, the kiln head of the rotary kiln (4) adopts oxygen enrichment technology, and the oxygen supply unit (13) can independently control the oxygen flow rate and pressure of the first branch (1601) and the second branch (1602). The oxygen flow rate of the first branch (1601) is calculated by back-calculating the fuel air volume and the target oxygen concentration of the third pipeline after oxygen enrichment, according to the following formula (1):

[0018] Where Q1 is the oxygen flow rate of the first branch (1601), in Nm³. 3 / h;Q mf The air volume of the fuel blower (11) is expressed in Nm³. 3 / h; α1 is the oxygen concentration after oxygen enrichment in the third pipeline (1603), in %; the oxygen concentration is adjusted according to the fuel properties provided by the fuel storage equipment (9), and the oxygen concentration α1 is controlled between 21% and 40%. This value takes into account the safety of the third pipeline. If the concentration is too high, the risk factor will increase; ε is the oxygen concentration provided by the oxygen supply unit (13), in %;

[0019] The oxygen flow rate of the second branch (1602) is obtained from the primary air volume and the target oxygen concentration of the fourth pipeline after oxygen enrichment, and is calculated according to the following formula (2):

[0020] Where Q2 is the oxygen flow rate of the second branch (1602), in Nm³. 3 / h;Q 1f The air volume of the primary air fan (12) is expressed in Nm³. 3 / h; α2 is the oxygen concentration after oxygen enrichment in the fourth pipeline (1604), in %; the oxygen concentration is adjusted according to the fuel properties provided by the first fuel storage equipment (9), and the oxygen concentration α2 is controlled between 21% and 45%.

[0021] Furthermore, the hydrogen supply flow rate of the hydrogen supply unit (14) to the decomposition furnace (2) is calculated according to the following formula (3): Q H =γ×Q cf (3)

[0022] Among them, Q H The hydrogen supply flow rate of the hydrogen supply unit (14) is expressed in Nm³. 3 / h; γ is the hydrogen coefficient, which is related to the properties of the fuel used in the decomposition furnace (2), and is 0.002 to 0.04. This value takes into account the hydrogen explosion limit (4% to 75%) and the fuel solid-gas ratio (3 to 5) to ensure that it is within the safe range. The range is determined according to the effect of hydrogen on most alternative fuels. When the hydrogen flow rate is greater than this value, it will compete with the alternative fuel for oxygen, resulting in poor combustion of the alternative fuel and causing the opposite effect; Q cf This refers to the fuel consumption at the kiln tail decomposition furnace, expressed in kg / h.

[0023] Furthermore, the distance σ between the hydrogen burner (201) and the tertiary air duct inlet (203) does not exceed 12m. This value is within the main combustion zone of the decomposition furnace, where the combustion reaction mainly occurs. Passing hydrogen through this zone ensures that hydrogen participates in the reaction. If the value is greater than this, although combustion still occurs, the hydrogen passing effect deteriorates, and the advantages of this method cannot be demonstrated.

[0024] Furthermore, hydrogen-rich technology is used at the decomposition furnace (2) at the kiln tail. One or more hydrogen burners (201) are provided. The hydrogen supply unit (14) is connected to the hydrogen burner (201) through one or more branches. The hydrogen supply unit (14) can control the hydrogen flow rate and pressure of each branch individually.

[0025] The advantages and positive effects of this invention are:

[0026] 1. This invention employs a hydrogen-rich and oxygen-rich calcination method for cement clinker. Using oxygen-rich combustion at the kiln head allows the use of only low-quality fuels at the kiln head, improving energy utilization, ensuring flame intensity, guaranteeing cement clinker quality, enriching the energy structure, and reducing dependence on high-quality fuels.

[0027] 2. The oxygen flow rate of the oxygen supply unit branch of the present invention can be adjusted according to the properties of the fuel used and the performance of the feed scale to ensure that the fuel is safely delivered to the kiln head burner and completely burned in the rotary kiln.

[0028] 3. This invention utilizes the characteristic of hydrogen to improve fuel combustion, using hydrogen as a final combustion agent, so that inferior fuel can be used completely at the kiln tail decomposition furnace, ensuring that the CO content in the flue gas at the decomposition furnace outlet is below 1000ppm, thus ensuring the complete combustion of inferior fuel at the decomposition furnace; the hydrogen coefficient γ is taken as 0.002 to 0.04, which can maximize the effect of hydrogen under safe hydrogen use conditions.

[0029] 4. The method of calcining cement clinker with hydrogen and oxygen enrichment of the present invention can increase the flame temperature at the kiln head, promote the complete combustion of fuel at the kiln head and kiln tail, and improve energy utilization; it has the conditions to optimize the air supply of the calcination system, reduce system resistance, increase system output, reduce heat consumption and electricity consumption, and achieve carbon emission reduction, thus having good economic and social benefits. Attached Figure Description

[0030] Figure 1 is a schematic diagram of a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods provided in an embodiment of the present invention;

[0031] Figure 2 is a schematic diagram of the interface of the kiln head burner provided in an embodiment of the present invention.

[0032] In the diagram: 1. Preheating unit; 2. Decomposition furnace; 201. Hydrogen burner; 202. Decomposition furnace burner; 203. Tertiary air duct inlet; 3. Smoke chamber; 4. Rotary kiln; 5. Kiln head burner; 501. Fuel air inlet; 502. Axial primary air inlet; 503. Swirl primary air inlet; 6. Kiln hood; 7. Cooler; 8. Tertiary air duct; 9. Fuel storage equipment; 10. Feed scale; 11. Fuel blower; 12. Primary air blower; 13. Oxygen supply unit; 14. Hydrogen supply unit; 15. Secondary energy supply unit. Detailed Implementation

[0033] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are within the scope of protection of the present invention.

[0034] In the description of this invention, it should be noted that the terms "upper," "lower," "inner," "outer," "top / bottom," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing the invention and for simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0035] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installed," "equipped with," "sleeved / connected," "connected," etc., should be interpreted broadly. For example, "connection" can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium; it can be a connection within two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0036] As shown in Figures 1 and 2, this embodiment provides a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods, including the following steps:

[0037] The raw materials are preheated in preheating unit 1;

[0038] The preheated raw materials are decomposed in decomposition furnace 2;

[0039] The raw materials after calcination and decomposition in rotary kiln 4;

[0040] The calcined cement clinker is cooled in cooler 7;

[0041] Oxygen-enriched combustion is adopted at the kiln head of rotary kiln 4. The oxygen-enriched combustion mode is realized by a first energy supply unit and an oxygen supply unit 13. The first energy supply unit includes a fuel storage device 9, a feed scale 10, a fuel supply fan 11, and a primary air fan 12. The fuel storage device 9, the feed scale 10, and the fuel air interface 501 of the kiln head burner 5 are connected in sequence. The fuel supply fan 11 is connected to the feed scale 10 through a third pipeline 1603. The primary air fan 12 is connected to the axial primary air interface 502 and the swirl primary air interface 503 of the kiln head burner 5 through a fourth pipeline 1604. The oxygen supply unit 13 is connected to the third pipeline 1603 through a first branch 1601 to increase the oxygen concentration in the fuel supply air. The oxygen supply unit 13 is connected to the fourth pipeline 1604 through a second branch 1602 to increase the oxygen concentration in the primary air.

[0042] Hydrogen-rich combustion is adopted in the decomposition furnace 2. The decomposition furnace 2 is equipped with a hydrogen burner 201, a decomposition furnace burner 202 and a tertiary air duct inlet 203. The hydrogen burner 201 is located above the tertiary air duct inlet 203. The hydrogen-rich combustion mode is realized by the hydrogen supply unit 14, which is connected to the hydrogen burner 201 and supplies hydrogen to the decomposition furnace 2 through the hydrogen burner 201 on the decomposition furnace 2.

[0043] The second power supply unit 15 is connected to the decomposition furnace burner 202 and supplies power to the decomposition furnace 2 through the decomposition furnace burner 202 on the decomposition furnace 2.

[0044] The fuel storage device 9 provides fuel with a calorific value of not less than 3500 kcal / kg and a moisture content of not more than 5%.

[0045] The second power supply unit 15 provides fuel with a calorific value of not less than 2000 kcal / kg and a moisture content of not more than 30%.

[0046] The kiln head of rotary kiln 4 adopts oxygen enrichment technology. The oxygen supply unit 13 can independently control the oxygen flow rate and pressure of the first branch 1601 and the second branch 1602. The oxygen flow rate of the first branch 1601 is calculated by back-calculating the fuel air volume and the target oxygen concentration of the third pipeline after oxygen enrichment, according to the following formula (1):

[0047] Where Q1 is the oxygen flow rate of the first branch 1601, in Nm³. 3 / h;Qmf The air volume of fuel blower 11 is expressed in Nm³. 3 / h; α1 is the oxygen concentration after oxygen enrichment in the third pipeline 1603, in %; the oxygen concentration is adjusted according to the fuel properties provided by the fuel storage equipment 9, and the oxygen concentration α1 is controlled between 21% and 40%. This value takes into account the safety of the third pipeline. If the concentration is too high, the risk factor will increase; ε is the oxygen concentration provided by the oxygen supply unit 13, in %;

[0048] The oxygen flow rate of the second branch 1602 is obtained from the primary air volume and the target oxygen concentration of the fourth pipeline after oxygen enrichment, and is calculated according to the following formula (2):

[0049] Where Q2 is the oxygen flow rate of the second branch 1602, in Nm³. 3 / h;Q 1f The air volume of primary air fan 12 is expressed in Nm³. 3 / h; α2 is the oxygen concentration after oxygen enrichment in the fourth pipeline 1604, in %; the oxygen concentration is adjusted according to the fuel properties provided by the first fuel storage device 9, and the oxygen concentration α2 is controlled between 21% and 45%.

[0050] The hydrogen supply flow rate of the hydrogen supply unit 14 to the decomposition furnace 2 is calculated according to the following formula (3): Q H =γ×Q cf (3)

[0051] Among them, Q H The hydrogen supply flow rate of hydrogen supply unit 14 is expressed in Nm³. 3 / h; γ is the hydrogen coefficient, which is related to the fuel properties used in decomposition furnace 2, and ranges from 0.002 to 0.04. This value takes into account the hydrogen explosion limit (4% to 75%) and the fuel solid-gas ratio (3 to 5) to ensure it is within a safe range. The range is determined based on the interaction between hydrogen and most alternative fuels. If the hydrogen flow rate exceeds this value, it will compete with the alternative fuel for oxygen, resulting in poor combustion of the alternative fuel and causing the opposite effect; Q cf This refers to the fuel consumption at the kiln tail decomposition furnace, expressed in kg / h.

[0052] The distance σ between the hydrogen burner 201 and the tertiary air duct inlet 203 does not exceed 12m. This value is within the main combustion zone of the decomposition furnace, where the combustion reaction mainly occurs. Passing hydrogen through this zone ensures that hydrogen participates in the reaction. If the distance exceeds this value, although combustion still occurs, the hydrogen passing effect deteriorates, and the advantages of this method cannot be demonstrated.

[0053] The decomposition furnace 2 at the kiln tail uses hydrogen-rich technology. One or more hydrogen burners 201 are provided. The hydrogen supply unit 14 is connected to the hydrogen burner 201 through one or more branches. The hydrogen supply unit 14 can control the hydrogen flow rate and pressure of each branch individually.

[0054] To better understand the above technical solution, the following will provide a detailed explanation of the technical solution in conjunction with the accompanying drawings and specific implementation methods.

[0055] Example 1

[0056] The method of this invention is applied to a 5000t / d cement clinker production line. This embodiment provides a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods. The hydrogen supply unit 14 is connected to the decomposition furnace 2 via a pipeline, and the decomposition furnace 2 has a hydrogen burner 201. Operating parameters are shown in Table 1.

[0057] Table 1 Operating Parameters

[0058] After this embodiment is implemented, the system resistance is reduced by 300Pa, the output is increased by 500t / d, the heat consumption is reduced by 6.5kgce / t.cl, the power consumption is reduced by 2kW·h / t.cl, and the carbon emission is reduced by 150.8kgCO2 / t.cl.

[0059] Example 2

[0060] The method of this invention is applied to a 5000t / d cement clinker production line. This embodiment provides a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods. The hydrogen supply unit 14 is connected to the decomposition furnace 2 via a pipeline, and the decomposition furnace 2 has a hydrogen burner 201. Operating parameters are shown in Table 2.

[0061] Table 2 Operating Parameters

[0062] After this embodiment is implemented, the system resistance is reduced by 220 Pa, the output is increased by 200 t / d, the heat consumption is reduced by 4.5 kgce / t.cl, the power consumption is reduced by 1.6 kW·h / t.cl, and the carbon emissions are reduced by 122.9 kg CO2 / t.cl.

[0063] Example 3

[0064] This invention is applied to an 8000t / d cement clinker production line. This embodiment provides a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods. The hydrogen supply unit 14 is connected to the decomposition furnace 2 via four branch lines. The decomposition furnace 2 has four hydrogen burners 201. The four hydrogen burners 201 are evenly distributed along the circumferential plane of the decomposition furnace 2 at an angle of 90°. Operating parameters are shown in Table 3.

[0065] Table 3 Operating Parameters

[0066] After this embodiment was implemented, the system resistance was reduced by 135 Pa, the output increased by 107 t / d, the heat consumption was reduced by 5 kgce / t.cl, and the carbon emissions were reduced by 132.3 kg CO2 / t.cl.

[0067] Example 4

[0068] This invention is applied to a 10,000 t / d cement clinker production line. This embodiment provides a method for calcining cement clinker using hydrogen-rich and oxygen-rich methods. The hydrogen supply unit 14 is connected to the decomposition furnace 2 via three branch lines. The decomposition furnace 2 has three hydrogen burners 201. The three hydrogen burners 201 are evenly distributed along the circumferential plane of the decomposition furnace 2 at an angle of 120°. The distance from one branch hydrogen burner to the tertiary air duct inlet 203 is 1.5 m, the distance from the second branch hydrogen burner to the tertiary air duct inlet 203 is 4.7 m, and the distance from the third branch hydrogen burner to the tertiary air duct inlet 203 is 11 m. The hydrogen supply unit is a water electrolysis device powered by a waste heat boiler. Operating parameters are shown in Table 4.

[0069] Table 4 Operating Parameters

[0070] After this embodiment is implemented, the system resistance is reduced by 340 Pa, the heat consumption is reduced by 7.5 kgce / t.cl, and the power consumption is reduced by 2.2 kW·h / t.cl.

[0071] The embodiments described above are only used to illustrate the technical ideas and features of the present invention. Their purpose is to enable those skilled in the art to understand the content of the present invention and implement it accordingly. The patent scope of the present invention should not be limited by these embodiments. That is, all equivalent changes or modifications made in accordance with the spirit disclosed in the present invention still fall within the patent scope of the present invention.

Claims

1. A method for calcining cement clinker with hydrogen-rich and oxygen-rich, comprising the following steps: preheating raw meal in a preheating unit (1); decomposing the preheated raw meal in a decomposing furnace (2); calcining the decomposed raw meal in a rotary kiln (4); cooling the calcined cement clinker in a cooler (7); characterized in that oxygen-rich combustion is adopted at the kiln head of the rotary kiln (4), and the oxygen-rich combustion mode is realized by a first energy supply unit and an oxygen supply unit (13), the first energy supply unit comprises a fuel storage device (9), a feeding scale (10), a fuel feeding fan (11) and a primary air fan (12), the fuel storage device (9), the feeding scale (10) and a fuel air interface (501) of a kiln head burner (5) are connected in sequence, the fuel feeding fan (11) is connected to the feeding scale (10) through a third pipeline (1603), and the primary air fan (12) is connected to an axial primary air interface (502) and a cyclone primary air interface (503) of the kiln head burner (5) through a fourth pipeline (1604); the oxygen supply unit (13) is connected to the third pipeline (1603) through a first branch (1601), and the oxygen supply unit (13) is connected to the fourth pipeline (1604) through a second branch (1602); hydrogen-rich combustion is adopted in the decomposing furnace (2), and a hydrogen energy burner (201), a decomposing furnace burner (202) and a tertiary air pipe access (203) are arranged on the decomposing furnace (2), the hydrogen energy burner (201) is located above the tertiary air pipe access (203); the hydrogen-rich combustion mode is realized by a hydrogen supply unit (14) connected to the hydrogen energy burner (201); a second energy supply unit (15) is connected to the decomposing furnace burner (202).

2. The method of claim 1, wherein the hydrogen-rich oxygen-rich calcined cement clinker is characterized by, The fuel storage device (9) provides fuel with a calorific value of not less than 3500 kcal / kg and a moisture content of not more than 5%.

3. The method of claim 1, wherein the hydrogen-rich oxygen-rich calcined cement clinker is characterized by, The second energy supply unit (15) provides fuel with a calorific value of not less than 2000 kcal / kg and a moisture content of not more than 30%.

4. The method of claim 1, wherein the hydrogen-rich oxygen-rich calcined cement clinker is characterized by, The oxygen supply unit (13) can separately control the oxygen flow and pressure of the first branch (1601) and the second branch (1602); The oxygen flow rate of the first branch (1601) is calculated according to the following formula (1): Q1 is the oxygen flow of the first branch (1601) in Nm3 / h 3 Q1 is the oxygen flow of the first branch (1601) in Nm3 / h mf Q1 is the oxygen flow of the first branch (1601) in Nm3 / h 3 Q1 is the oxygen flow of the first branch (1601) in Nm3 / h The oxygen supply unit (13) provides oxygen with a concentration of %; The oxygen flow rate of the second branch (1602) is calculated according to the following equation (2): Q2 is the oxygen flow of the second branch (1602) in Nm 3 / h; Q 1f Q is the air volume of the primary air fan (12) in Nm 3 / h; α2 is the oxygen concentration of the fourth pipeline (1604) after enrichment, and α2 is 21% to 45%.

5. The method of claim 1, wherein the hydrogen-rich oxygen-rich calcined cement clinker is characterized by, The hydrogen supply unit (14) has a hydrogen supply flow rate calculated according to the following formula (3): Q H = γ x Q cf (3) wherein Q H is the hydrogen supply flow rate of the hydrogen supply unit (14) in Nm 3 / h; γ is the hydrogen coefficient, which is 0.002-0.04; Q cf is the fuel consumption of the decomposition furnace in kg / h.

6. The method of claim 1, wherein the hydrogen-rich oxygen-rich calcined cement clinker is characterized by, The distance σ between the hydrogen energy burner (201) and the tertiary air pipe access (203) is not more than 12 m.

7. The method of claim 1, wherein the hydrogen-rich oxygen-rich calcined cement clinker is characterized by, One or more hydrogen energy burners (201) are arranged, and the hydrogen supply unit (14) is connected to the hydrogen energy burner (201) through one or more branches, and the hydrogen supply unit (14) can separately control the hydrogen flow and pressure of each branch.

Images