Process and device for flash reduction modification of molten iron-containing slag
By using a flash reduction modification process for molten iron-containing slag, hydrogen-rich gas and ammonia are rapidly reacted with the molten iron-containing slag under negative pressure or in a closed state. This solves the problems of high energy consumption and difficulty in resource utilization in existing technologies, achieves efficient recovery of iron and other metals, reduces energy consumption and reducing agent consumption, and improves the resource utilization rate and quality of the product.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-12-18
- Publication Date
- 2026-03-27
AI Technical Summary
Existing technologies for treating molten iron-containing smelting slag suffer from problems such as high energy consumption, difficulty in utilizing iron products as resources, and difficulty in manufacturing slag-making equipment. Furthermore, traditional methods require high modification temperatures and large amounts of reagents for molten slag, resulting in low metal recovery rates and severe environmental pollution.
The flash reduction and upgrading process of molten iron-containing slag is adopted. By mixing reducing coal, sulfiding agent and slag-forming agent, hydrogen-rich gas and ammonia gas react rapidly with molten iron-containing slag under negative pressure or closed state to reduce the viscosity of molten slag and perform jet water cooling granulation. Then, magnetic separation and flotation separation are carried out to obtain high-quality iron products.
It achieves efficient recovery of iron and other metals, reduces energy consumption and reducing agent consumption, reduces environmental pollution, and improves the resource utilization rate and quality of products.
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Figure CN121737459A_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The present application relates to the field of resource utilization of molten iron-containing smelting slag, in particular, and especially relates to a process and device for flash reduction and modification of molten iron-containing slag. BACKGROUND
[0002] More than one hundred million tons of iron-containing smelting slag, such as copper-nickel slag, lead-zinc slag, and steel smelting slag, are generated annually in the production process of metal ore smelting in the smelting industry. A large amount of hot-state iron-containing smelting slag is usually generated in a smelting furnace in a traditional pyrometallurgical process. For example, the temperature of copper blowing slag is 1150-1250℃, and the iron content is 35-40%; the temperature of lead smelting slag (containing lead smelting slag or fuming furnace slag) is more than 1100℃, and the iron content is more than 21%; and the temperature of steel slag can be more than 1500℃, and the iron content is more than 20%.
[0003] As solid waste, if the iron-containing smelting slag cannot be properly and effectively disposed of, it will not only be a waste of resources, but also cause a series of environmental problems. Under the background of the increasingly tight mineral resources and the increasingly strict environmental regulations, it is of great strategic significance to realize the "reduction, resource utilization, and harmlessness" treatment of iron-containing smelting slag and efficiently recover valuable elements therein, so as to ensure the safety of metal resources in China and promote the green and low-carbon cyclic development of the smelting industry.
[0004] At present, the methods for solving molten iron-containing smelting slag are divided into direct treatment of hot-state slag and post-treatment of cold-state slag. The direct treatment of hot-state slag is divided into two categories, namely, fire-based depletion and fire-based sulfidation. In the former, coke, sulfidation agent, CaO, B2O3, and the like are added to the smelting slag for oxidation modification, and in the latter, the smelting slag is heated and then a sulfidation agent is added to re-create a matte. The common shortcomings of the two methods are that the iron-containing smelting slag is continuously heated as a whole, the modification temperature is high, and the amount of reagent added is large. The fire-based depletion also has the shortcomings of high magnetite content, difficulty in remelting utilization, difficulty in controlling foamed slag, and difficulty in subsequent separation, while the smelting slag for creating matte also has the major problems of difficulty in subsequent utilization of metallic matte melt and difficulty in manufacturing of corresponding equipment, and there is still no mature industrialized smelting device for creating matte from slag. If the post-treatment of cold-state slag is adopted, the iron-containing slag is cooled and then separated and recovered by beneficiation. The disadvantage is that iron is mostly mixed with silicate in the form of fayalite phase, the recovery rate of beneficiation is low, and a large amount of remaining tailings has low activity and can only be used as raw materials for building materials and the like, and can only be disposed of by stacking. Moreover, the tailings after grinding and flotation have very fine particle size, are easy to fly and disperse, and increase the stacking cost. Therefore, it is of great practical significance to realize effective resource utilization of molten iron-containing smelting slag for the sustainable development of the smelting industry. SUMMARY
[0005] In view of the problems in the prior art, such as high energy consumption, difficulty in resource utilization of iron products, and difficulty in manufacturing of smelting slag equipment, the present application provides a process and device for flash reduction and modification of molten iron-containing slag. The specific process and device include the following contents:
[0006] S1. Mix the reducing coal, sulfuration agent and slagging agent according to the required mass of the slag.
[0007] S2. Molten iron-bearing slag jet reduction modification: pass the preheated hydrogen-rich gas through the No. 1 injector into the molten slag bin, then add the molten iron-bearing slag into the nozzle of the No. 1 injector, add the modification agent to the hydrogen-rich gas and flush it into the mixing chamber of the No. 1 injector, and quickly mix and react the hydrogen-rich gas with the molten iron-bearing slag, then pass the reacted melt into the molten slag bin through the feeding pipe and keep it for a period of time.
[0008] S3. Jet water cooling granulation: add the kept melt into the nozzle of the No. 2 injector of the cooling bin, pass the room temperature saturated ammonia water solution into the mixing chamber of the No. 2 injector, and quickly mix and cool the molten slag, then continue to cool and granulate the slag after the slag is thrown by the centrifugal disc in the cooling bin. The generated high-temperature ammonia gas is recycled after heat utilization and water absorption.
[0009] S4. Mineral separation: grind the granulated slag, then magnetically separate it to obtain a magnetic iron product, and then separate the remaining slag into iron concentrate and silicate slag by flotation.
[0010] Preferably, the reducing coal in step S1 is one or more of anthracite, lignite and biomass charcoal, the particle size is less than 1 mm, and the addition amount is 0.5% to 10% of the mass of the slag.
[0011] Preferably, the sulfuration agent in step S1 is one or more of pyrite, sulfur, chalcopyrite, sodium sulfide and organic sulfur which can form elemental sulfur, the particle size is less than 1 mm, and the addition amount is 0.5% to 10% of the mass of the slag.
[0012] Preferably, the slagging agent in step S1 is one or more of lime, fluorite, carbide and bauxite, the particle size is less than 1 mm, and the addition amount is 5% to 25% of the mass of the slag.
[0013] Preferably, the molten iron-bearing slag in step S2 is one or more of molten copper slag, nickel slag, lead slag, zinc slag, iron slag and steel slag, and the iron content is 10% to 50%.
[0014] Preferably, the preheated hydrogen-rich gas in step S2 has a hydrogen content of 90% to 100%, a preheating temperature of 400 to 1200℃, and a gas pressure of 0.10 to 0.15 Mpa.
[0015] Preferably, the molten slag bin in step S2 has a keeping temperature of 1050 to 1450℃, a keeping time of 15 to 120 min, and ammonia gas is passed into the injector during the keeping process. The keeping process only maintains the original molten state temperature without additional heating.
[0016] Preferably, the cooling bin in step S3 is externally provided with a jacketed water-cooled wall, and the cooling water passes through the water-cooled wall to further cool the molten slag.
[0017] Preferably, the rotating disc in step S3 rotates at a speed of 100-800 rpm.
[0018] Preferably, the particle size of the ground slag particles in step S4 is less than 74 microns, accounting for 75-100%.
[0019] The present application adopts the above-mentioned process and device for flash reduction and modification of molten iron-containing slag, and the following beneficial effects can be achieved:
[0020] (1) High recovery rate of iron and other metals. The existing iron-containing molten slag is mainly oxidized and modified, but the oxygen in the iron-containing molten slag has already reached saturation during the smelting process, and further oxidation and modification will result in more sticky slag and lower metal recovery rate. The present application quickly completes the reduction and modification of the slag in a reducing atmosphere, reduces the viscosity of the molten slag, and improves the metal recovery rate.
[0021] (2) Low energy consumption. There is no need for additional heating of the slag, and only the molten state needs to be maintained. If the iron-containing smelting slag is completely treated by a coking smelting process, a large amount of reducing agent needs to be consumed, and the coking process needs to re-bond and absorb a large amount of heat, so the molten slag needs to be reheated and smelted. However, due to the low content of valuable components other than iron in the product, the return of coking iron to the main smelting system has poor economic benefits and high energy consumption. The present application does not need to additionally heat the slag, and the target product is not a single sulfide, so the energy consumption is greatly reduced.
[0022] (3) Low consumption of reducing agent. Unlike the existing complete hydrogen reduction process of molten slag, the present application only passes in hydrogen-rich gas during the flash reduction of molten slag, and uses ammonia and ammonia water respectively in the stages of heat preservation and water cooling, greatly reducing the consumption of expensive hydrogen reducing agent and abandoning the harsh pressurized reduction conditions, thus reducing the cost.
[0023] (4) High product quality. The iron product after modification and reduction is easy to separate, and the resource utilization capacity is greatly improved.
[0024] (5) No sulfur dioxide gas. No sulfur dioxide gas is generated in the hydrogen and ammonia atmosphere, and the whole process is completed in a negative pressure or closed state, effectively solving the problem of environmental pollution. BRIEF DESCRIPTION OF DRAWINGS
[0025] In order to more clearly illustrate the technical scheme of the product of the present application, the drawings of the present application are briefly introduced as follows. The drawings, together with the specific embodiments below, are used to explain the present application, but do not constitute a limitation on the present application.
[0026] Figure 1 Process flow chart of the process and device for flash reduction and modification of molten iron-containing slag according to the present application.
[0027] Figure 2 Schematic diagram of the jet flow reduction and modification reaction chamber for molten iron-containing slag according to the present application, wherein: 1 - slag pouring funnel; 2 - compressed nitrogen; 3 - modification agent pouring port; 4 - slag inlet valve; 5 - No. 1 injector; 6 - modification agent pouring valve; 7 - hydrogen-rich gas / ammonia gas inlet; 8 - molten slag bin; 9 - molten slag outlet valve. The injection speed of molten slag in the bin is adjusted by compressed nitrogen.
[0028] Figure 3 Schematic diagram of the jet flow water-cooling granulation reaction chamber for molten iron-containing slag according to the present application, wherein: 10 - slag pouring funnel; 11 - compressed nitrogen; 12 - cooling ammonia water inlet; 13 - slag inlet valve; 14 - No. 2 injector; 15 - high-temperature ammonia gas outlet; 16 - cooling jacket; 17 - cooling bin; 18 - rotating disc; 19 - granulated slag outlet valve. The injection speed of molten slag in the bin is adjusted by compressed nitrogen. DETAILED DESCRIPTION
[0029] The present application will be further described in detail below in conjunction with the embodiments and the accompanying drawings, wherein the reference signs correspond to the reference signs of the devices in the accompanying drawings. Figure 2 and the accompanying drawings. Figure 3 However, the protection scope of the present application is not limited thereto.
[0030] The ranges and values indicated herein are not limited thereto, and these ranges should be understood as including values close to and around these ranges or values, which do not make substantial improvements and adjustments to the present application and still belong to the protection scope of the present application.
[0031] Example 1
[0032] The molten iron-containing slag to be treated is molten copper slag, and the main components of the molten copper slag are: Cu 2.35wt%, TFe 50.0wt%, S 0.48wt%, Zn 1.35wt%, Pb 1.24wt%, SiO2 27.66wt%, CaO 5.31wt%, Al2O3 2.62wt%, MgO 0.48wt%, FeO 0.48wt%, Fe2O3 0.48wt%, Fe3O4 0.48wt%, FeO·Fe2O3 0.48wt%, FeO·Fe3O4 0.48wt%, FeO·Fe2O3·Fe3O4 0.48wt%, and the like.
[0033] 6.34wt%, MgO 0.29wt%, copper slag temperature 1250℃. First, mix the anthracite, pyrite and lime according to 10%, 10% and 25% of the relative molten copper slag quality respectively, and the particle size of all particles in the mixture is less than 1mm. After the completion of the mixing, place the mixture into the modified agent pouring port 3, close the valves 4 and 6, and then add the molten copper slag into the slag pouring funnel 1. Pass the preheated hydrogen-rich gas (hydrogen content is 100%, temperature is 1200℃, and gas pressure is 0.15Mpa) into the slag tank through the first injector, and then open the valve 4 at the same time, so that the molten iron-containing slag is added into the nozzle of the first injector through the slag pouring funnel 1, and the flow rate is controlled by compressed nitrogen. Open the valve 6, add the mixed modified agent into the hydrogen-rich gas, and then flush into the mixing chamber of the first injector with the hydrogen-rich gas to rapidly mix and react with the molten iron-containing slag. The reacted melt is passed into the slag tank 8 through the feeding pipe, and is kept at 1250℃ for 15min. During the keeping process, the valves 4 and 6 are closed, and the hydrogen-rich gas is replaced by ammonia gas. The keeping process only maintains the original molten state temperature without additional heating. The kept melt is added into the nozzle of the cooling tank second injector through the slag pouring funnel 11, and the room temperature saturated ammonia water solution is passed into the mixing chamber of the second injector to rapidly mix and cool with the molten slag. The slag is further cooled and granulated after being thrown by the rotating disc in the cooling tank, and the rotating speed of the rotating disc is 800rpm. The high-temperature ammonia gas generated in the cooling tank is used after heat utilization, absorbed by water, and then recycled. The obtained granulated slag is ground to a particle size of less than 74 microns, and then the elemental iron product is obtained by magnetic separation. The remaining slag is further separated into iron concentrate and calcium silicate slag by flotation. After analyzing and calculating the iron and copper in the product, the total recovery rates of iron and copper are 91.95% and 90.36% respectively, the yield of elemental iron powder is more than 30%, the flotation recovery rate of iron concentrate is 90.78%, the iron grade of the iron concentrate is 85.39%, and the heavy metal content in the calcium silicate tailings is less than 0.15%. The products can be directly recycled and utilized.
[0034] Comparative Example 1
[0035] The molten iron-containing slag to be treated is the same as in Example 1, and the modified agent with the same quality and composition as in Example 1 is added in the slag package under stirring. After keeping at 1250℃ for 15min, the existing traditional water quenching-grinding-magnetic separation-flotation process is used to obtain the iron concentrate and tailings products. Through analysis and calculation, the total recovery rates of iron and copper are 30.31% and 36.21% respectively, the iron grade in the iron concentrate is 63.37%, and the copper content in the tailings is 0.25%. There is still a large amount of magnetite in the iron concentrate product which is wrapped by ferrosilicon and is difficult to utilize. A large amount of acidic smoke with pollution is generated immediately after the modified agent is added. According to the comparison results, the present application can achieve the effects of higher product recovery rate, lower product impurity content, higher product recycling utilization degree, and effective pollution reduction.
[0036] Example 2
[0037] The molten iron-containing slag to be treated is molten lead-zinc slag, and the main components of the molten lead-zinc slag are: TFe 10.0wt%, S 10.16wt%, Zn 6.84wt%, Pb 0.49wt%, SiO2 12.29wt%, and the temperature of the lead-zinc slag is 1050℃. First, mix the mixture of lignite, sulfur and sodium sulfide (mass ratio 1:1), the mixture of fluorite and lime (mass ratio 1:2) respectively according to 0.5%, 0.5% and 5% of the relative mass of the molten lead-zinc slag, and the particle size of all particles in the mixture is less than 1mm. After the mixing is completed, place the modifier in the modifier pouring port 3, close the valves 4 and 6, and then add the molten lead-zinc slag to the slag pouring funnel 1. Preheated hydrogen-rich gas (hydrogen content is 90%, temperature is 400℃, gas pressure is 0.10Mpa) is introduced into the slag tank through the first injector, and then the valve 4 is opened at the same time, so that the molten lead-zinc slag is added into the spray pipe of the first injector through the slag pouring funnel 1, and the flow rate is controlled by compressed nitrogen. Open the valve 6, add the mixed modifier to the hydrogen-rich gas and flush it into the mixing chamber of the first injector with the hydrogen-rich gas, and then mix and react rapidly with the molten lead-zinc slag. The reacted melt is introduced into the slag tank 8 through the feed pipe and kept at 1050℃ for 120min. During the holding process, the valves 4 and 6 are closed and the hydrogen-rich gas is replaced by ammonia gas. The holding process only maintains the original molten state temperature without additional heating. The molten slag after holding is added into the spray pipe of the cooling tank two injector, and the room temperature saturated ammonia water solution is introduced into the mixing chamber of the two injector to rapidly mix and cool with the molten slag. The slag is further cooled and granulated after being thrown by the rotating disc in the cooling tank, and the rotating speed of the rotating disc is 100rpm.
[0038] The high-temperature ammonia gas generated in the cooling tank is used after heat utilization, absorbed by water and then returned for recycling. The obtained granular slag is ground to a particle size of less than 74 microns, and the elemental iron product is obtained by magnetic separation. The remaining slag is further separated into iron concentrate and calcium silicate slag by flotation. After analyzing and calculating the iron in the product, the total recovery rate of iron reaches 95.35%, the yield of elemental iron powder is more than 60%, the flotation recovery rate of iron concentrate is 91.55%, the iron grade of iron concentrate is 90.21%, and the content of lead, zinc and other heavy metals in calcium silicate tailings is less than 0.10%. The formed products can be directly recycled and utilized.
[0039] Comparative Example 2
[0040] The molten iron-containing slag to be treated is the same as in Example 2, and after grinding, granulation is performed together with coal (coal blending amount 10%), reduction is performed in a rotary kiln at 1050°C for 120 min, and then the existing conventional water quenching-magnetic separation-flotation process is used to obtain iron concentrate and tailing products. Through analysis and calculation, the total iron recovery rate reaches 83.51%, the iron grade in the iron concentrate is 36.41%, and the lead and zinc content in the tailings is more than 0.83%. There is still a large amount of iron silicate in the iron concentrate product, and the lead and zinc content is high and difficult to utilize. Compared with Comparative Example 2, the energy consumption of Example 2 is reduced by 80%, and the reducing agent consumption is reduced by 75%. According to the comparison results, the present application can achieve the effects of higher product recovery rate, lower product impurity content, higher product resource utilization degree, lower energy consumption, and smaller reducing agent consumption.
[0041] Example 3
[0042] The molten iron-containing slag to be treated is a mixture of molten steel slag, iron slag and nickel slag. The main components of the molten iron-containing slag are: TFe 22.98wt%, SiO2 18.21wt%, CaO 39.74wt%, Al2O3 5.41wt%, MgO 4.57wt%, and the temperature of the molten iron-containing slag is 1450℃. First, mix the mixture of anthracite and biomass charcoal (mass ratio 1:0.5), the mixture of pyrite and organic sulfur (mass ratio 1:0.3), and the mixture of lime fluorite and carbide (mass ratio 1:1:1) according to 5.2%, 3.5% and 20.3% of the relative mass of the molten iron-containing slag, respectively. The particle size of all the materials in the mixture is less than 1mm. After the mixing is completed, place the mixture in the modified agent pouring port 3, close the valves 4 and 6, and then add the molten copper slag to the slag pouring funnel 1. Preheat the hydrogen-rich gas (hydrogen content is 97.5%, temperature is 1175℃, and gas pressure is 0.13Mpa) and pass it into the slag tank through the first injector. Then, open the valve 4 to make the molten iron-containing slag pass through the slag pouring funnel 1 and enter the nozzle of the first injector, and control the flow rate with compressed nitrogen. Open the valve 6 to add the mixed modified agent to the hydrogen-rich gas and flush it into the mixing chamber of the first injector along with the hydrogen-rich gas to rapidly mix and react with the molten iron-containing slag. The reacted melt enters the slag tank 8 through the feed pipe and is kept at 1450℃ for 96min. During the holding process, close the valves 4 and 6 and change the hydrogen-rich gas to ammonia gas. The holding process only maintains the original molten state temperature without additional heating. After holding, the melt is added to the nozzle of the cooling tank second injector through the slag pouring funnel 11, and the room temperature saturated ammonia water solution is passed into the mixing chamber of the second injector to rapidly mix and cool with the molten slag. The slag is further cooled and granulated after being thrown by the rotating disc in the cooling tank, and the rotating speed of the rotating disc is 562rpm. The high-temperature ammonia gas generated in the cooling tank is used for heat utilization, then absorbed by water and recycled. The obtained granulated slag is ground to a particle size of less than 74 microns, accounting for 89%, and the elemental iron product is obtained by magnetic separation. The remaining slag is further separated into iron concentrate and calcium silicate slag by flotation. After analyzing and calculating the iron and copper in the product, the total recovery rates of iron and nickel are 90.72% and 95.61%, respectively. The yield of elemental iron powder is more than 75%, the flotation recovery rate of iron concentrate is 92.24%, the iron grade of iron concentrate is 86.52%, and the heavy metal content in the calcium silicate tailings is less than 0.10%. The products formed can be directly recycled and utilized.
[0043] Comparative Example 3
[0044] The molten iron-containing slag to be treated is the same as in Example 1, hydrogen is introduced and reduction is carried out at 1450 DEG C for 120 minutes, and then the existing traditional water quenching-grinding-magnetic separation-flotation process is used to obtain iron concentrate and tailing products. Through analysis and calculation, the total recovery rates of iron and nickel are 80.32% and 83.51% respectively, the iron grade in the iron concentrate is 78.37%, and the nickel content in the tailings is 0.36%. Compared with Comparative Example 3, the energy consumption of Example 3 is reduced by 90%, the consumption of reducing agent is reduced by 80%, and the hydrogen operating pressure is reduced by 80%. According to the comparison results, the present application can achieve the effects of higher product recovery rate, lower product impurity content, high degree of product resource utilization, low energy consumption, and small consumption of reducing agent.
[0045] The above description is only the preferred embodiment of the present application, and is not intended to limit the present application in other forms. Any person skilled in the art can modify or change the above disclosed technical content into equivalent embodiments with equivalent changes. However, any simple modification, equivalent change and modification of the above embodiments made according to the technical essence of the present application without departing from the technical scheme of the present application still falls within the protection scope of the present application.
Claims
1. A process and apparatus for flash reduction modification of molten iron-containing slag, characterized in that: This process involves four parts: modifier mixing and batching, molten iron-containing slag jet reduction and modification, jet water-cooled granulation, and mineral processing and separation. The specific steps are as follows: S1. Modifier mixing and batching: The reducing coal, sulfiding agent and slag-forming agent are mixed and batched according to the mass required for the slag. S2. Molten iron slag jet reduction and modification: Preheated hydrogen-rich gas is introduced into the molten slag chamber through the No. 1 injector. Molten iron slag is then added into the nozzle of the No. 1 injector through the slag pouring funnel. Modifier is added to the hydrogen-rich gas and is rushed into the mixing chamber of the No. 1 injector along with the hydrogen-rich gas to quickly mix and react with the molten iron slag. The reacted melt enters the molten slag chamber through the feed pipe and is kept at a temperature for a period of time. S3. Jet-cooled granulation: The heated melt is added to the nozzle of the second injector in the cooling chamber. A room-temperature saturated ammonia solution is then introduced into the mixing chamber of the second injector to rapidly mix with the molten slag and cool it down. The slag is then further cooled and granulated after being scattered by a centrifugal disc in the cooling chamber. The generated high-temperature ammonia gas is recycled after being used for heat recovery and absorbed by water. S4. Mineral processing and separation: After grinding the granular slag, magnetic separation is first performed to obtain magnetic iron products. The remaining slag is then separated into iron concentrate and silicate slag by flotation.
2. The process and apparatus for flash reduction modification of molten iron-containing slag as described in claim 1, characterized in that: The reducing coal in step S1 is one or more of anthracite, lignite, and biochar, with a particle size of less than 1 mm, and the amount added is 0.5% to 10% of the slag mass.
3. The process and apparatus for flash reduction modification of molten iron-containing slag as described in claim 1, characterized in that: The sulfiding agent in step S1 is one or more of pyrite, sulfur, chalcopyrite, sodium sulfide, and organic sulfur that can form elemental sulfur, with a particle size of less than 1 mm, and the amount added is 0.5% to 10% of the mass of the slag.
4. The process and apparatus for flash reduction modification of molten iron-containing slag as described in claim 1, characterized in that: The slag-forming agent in step S1 is one or more of lime, fluorite, calcium carbide, and bauxite, with a particle size of less than 1 mm, and the amount added is 5% to 25% of the mass of the molten slag.
5. The process and apparatus for flash reduction modification of molten iron-containing slag as described in claim 1, characterized in that: The molten iron-containing slag in step S2 is one or more of molten copper slag, nickel slag, lead slag, zinc slag, iron slag and steel slag, with an iron content of 10% to 50%.
6. The process and apparatus for flash reduction modification of molten iron-containing slag as described in claim 1, characterized in that: The hydrogen content of the preheated hydrogen-rich gas in step S2 is 90% to 100%, the preheating temperature is 400 to 1200°C, and the gas pressure is 0.10 to 0.15 MPa.
7. The process and apparatus for flash reduction and modification of molten iron-containing slag as described in claim 1, characterized in that: The slag chamber in step S2 is kept at a temperature of 1050-1450°C for 15-120 minutes, and ammonia gas is introduced into the injector during the heat preservation process. The heat preservation process maintains the original molten state temperature without additional heating.
8. The process and apparatus for flash reduction modification of molten iron-containing slag as described in claim 1, characterized in that: In step S3, the cooling chamber is equipped with a jacketed water-cooled wall, through which cooling water further cools the molten slag.
9. The process and apparatus for flash reduction modification of molten iron-containing slag as described in claim 1, characterized in that: The rotational speed of the rotating disk in step S3 is 100-800 rpm.
10. The process and apparatus for flash reduction modification of molten iron-containing slag as described in claim 1, characterized in that: In step S4, the particle size of the granules after grinding is less than 74 micrometers, accounting for 75-100%.