A method for preventing drainage and blocking of a hydrogen-based vertical furnace gas separator

Abstract

The present invention relates to the technical field of hydrogen-based vertical furnace gas-liquid separation, and discloses a method for preventing drainage and clogging of a hydrogen-based vertical furnace gas separator, which specifically comprises the following steps: S1, installing a direct cooling water valve group on the upper part of a process gas quenching orifice plate, spraying high-pressure direct cooling water into the airflow through holes located on an inner tube, thereby cooling the gas; providing a dosing device on the direct cooling water supply main pipe, injecting a certain proportion of dispersant solution according to the amount of direct cooling water used, preventing the sedimentation and agglomeration of solid particles in the direct cooling water system in the process gas circuit, protecting the pipeline from scale erosion, and reducing the clogging of the separator drainage system; in the present invention, the process gas separator drainage valve group is equipped with a corresponding automatic control program, and the separator is automatically drained through parameter optimization, which can free manpower from the tense hydrogen-based vertical furnace smelting process, and at the same time can enhance the stability of the vertical furnace smelting, thereby realizing the automation of hydrogen-based vertical furnace smelting.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrogen-based vertical furnace gas-liquid separation, and more specifically discloses a method for preventing drainage and blocking of a hydrogen-based vertical furnace gas separator. Background Art

[0002] In the hydrogen-based shaft furnace gas process, high-temperature, high-pressure reducing gas is introduced into the shaft furnace gas chamber at the center of the shaft furnace. The reducing gas reacts with the oxidized pellets within the shaft furnace, and the gas discharged from the top of the shaft furnace is called top gas. The top gas exiting the shaft furnace enters the top gas heat exchanger for heat recovery. The gas exiting the top gas heat exchanger is called process gas. It enters the process gas quench plate for water scrubbing and then enters the process gas venturi for acceleration. This acceleration dissolves any solid particles entrained in the gas into the small water droplets.

[0003] The accelerated process gas enters the process gas separator to separate the liquid and dust entrained in the gas. At the bottom of the separator, the dust particles remain suspended in water; clean hot water is added to the conical part of the container to ensure that the solids do not settle on the container wall.

[0004] In existing vertical furnace production processes, the top gas carries a large amount of dust. After being scrubbed and accelerated by direct cooling water jets, solid particles are entrained in the liquid flow. The wastewater is collected in the conical section of the process gas separator and discharged back to the direct cooling water tank via the bottom drainage valve group for recycling. Due to the high dust content of the wastewater, sludge easily settles and accumulates at the bottom of the separator, clogging pipes and valves, hindering the smooth operation of the drainage system and even causing vertical furnace shutdown. Summary of the Invention

[0005] The present invention provides a method for preventing drainage and blocking of a hydrogen-based vertical furnace gas separator, which can solve the problems raised in the above-mentioned background technology.

[0006] To solve the above technical problems, according to one aspect of the present invention, more specifically, a method for preventing blockage in drainage of a hydrogen-based vertical furnace gas separator is provided. The method comprises configuring a dispersant dosing device, setting up a process water valve group, reducing scaling and sludge sedimentation inside the tower and pipelines, configuring an automatic control system for the process water valve group, and optimizing parameters to achieve smooth drainage of the separator and maintain stable production in the hydrogen-based vertical furnace. The method specifically comprises the following steps:

[0007] S1. Install a direct cooling water valve group on the upper part of the process gas quenching orifice plate. High-pressure direct cooling water is sprayed into the airflow through the holes on the inner tube to cool the gas. A dosing device is installed on the direct cooling water supply main pipe. A certain proportion of dispersant solution is injected according to the direct cooling water usage to prevent the sedimentation and aggregation of solid particles in the direct cooling water system in the process gas loop, protect the pipeline from scale erosion, and reduce the blockage of the separator drainage system.

[0008] S2. Two tangential inlets for flushing water are set in the conical part of the process gas separator. A set of high-pressure direct cooling water valves including a shut-off valve YSV120401 and a flow regulating valve FV120401 are set. 10-20m3 / h of direct cooling water is injected tangentially to continuously flush the conical part of the process gas separator to prevent solids and sludge from settling and getting stuck on the bottom cone. The washed process gas and water are discharged from the lower pipe.

[0009] S3. Four interfaces for liquid level transmitters are installed at the bottom of the process gas separator: one for control and three for the SIS safety system, namely LT120402 and LIT120401A / B / C. The container liquid level is controlled by valve LV120402A / B. There is a stop valve YSV120404 upstream controlled by the system interlock. When the liquid level control valves LV120402A / B are put into use simultaneously, LV120402A serves as the main valve and LV120402B serves as the auxiliary valve, adjusting the opening according to the liquid level. At the same time, the LV120402B auxiliary valve is designed with a timed valve opening control program, which opens the drain valve LV120402B to 100% every T hours. By increasing the drainage flow, the accumulated sludge solids due to long-term use of the valve are flushed, reducing clogging.

[0010] S4. After entering automatic control, set the process gas separator control liquid level parameter LY120401. According to the actual liquid level LV120401 measured by the liquid level gauge at the bottom of the process gas separator during the vertical furnace smelting process, compare the sizes of LY120401 and LV120401. The automatic program control instruction directly adjusts the opening of the liquid level control valve LV120402A / B to achieve process gas separator liquid level adjustment.

[0011] Furthermore, in step S4, the adjustment principle is: when LV120401 is less than LY120401, the opening of the regulating valve LV120402A / B is reduced to LV120401≈LY120401; when LV120401 is greater than LY120401, the opening of the regulating valve LV120402A / B is increased to LV120401≈LV120401.

[0012] Furthermore, in step S4, the determination principle of LV120401≈LY120401 is:

[0013] Let k = (LY120401-LV120401) / LY120401×100%. If the k value is between -10% and 10%, it is determined that LV120401≈LY120401; when LV120401≈LY120401, the opening of the regulating valve LV120402A / B is kept unchanged.

[0014] Furthermore, in step S4, if the k value is not equal to -10% to 10%, the opening of the liquid level control valve LV120402A / B is adjusted, and the valve position △h is adjusted each time. After the adjustment, it is maintained for t time, and then the size relationship between LV120401 and LY120401 is continuously determined until the k value is between -10% and 10%;

[0015] Among them, △h is a parameter related to the valve position of the liquid level control valve LV120402A / B. The system selects that the unit of t is s and the unit of △h is %.

[0016] Furthermore, in step S3, T is optimized and set in the automatic control program according to data related to process direct cooling water, and the unit is h.

[0017] Furthermore, in step S4, Δh=0.1%, and t=2S.

[0018] The beneficial effects of the drainage and anti-clogging method for a hydrogen-based vertical furnace gas separator of the present invention are:

[0019] In the present invention, a dosing device is provided to prevent the sedimentation and aggregation of solid particles, protect the pipeline from being corroded by scale, and reduce the blockage of the separator drainage system.

[0020] In the present invention, a set of direct cooling water flushing valve groups and bottom drainage control valve groups are provided for the tapered part of the separator to realize continuous flushing of the tapered section of the separator and discharge sludge and sewage from the lower container. The bottom drainage valve group controls the liquid level of the separator and switches regularly to reduce the possibility of blockage due to long-term use and extend the equipment maintenance cycle, thereby ensuring the smooth operation of the separator drainage system and maintaining stable production of the hydrogen-based vertical furnace.

[0021] In the present invention, the process gas separator drainage valve group is equipped with a corresponding automatic control program, which automatically realizes smooth drainage of the separator through parameter optimization, thereby freeing manpower from the tense hydrogen-based vertical furnace smelting process, and at the same time enhancing the stability of the vertical furnace smelting, thereby realizing automated, clean, efficient and stable production of hydrogen-based vertical furnace smelting. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] The present invention will be further described in detail below with reference to the accompanying drawings and specific implementation methods.

[0023] Figure 1 This is the process flow chart of the process gas separator;

[0024] Figure 2 This is a flow chart of the automatic control method of the process gas separator drain valve group. DETAILED DESCRIPTION

[0025] The present invention will be described in detail below with reference to the accompanying drawings and in combination with embodiments. It should be noted that, unless there is a conflict, the embodiments and features in the embodiments of the present application can be combined with each other.

[0026] According to the attached Figure 1-2 A method for preventing blockage and drainage of a hydrogen-based vertical furnace gas separator is provided. The method comprises configuring a dispersant dosing device, setting up a process water valve group, reducing scaling and sludge sedimentation inside the tower and pipelines, configuring an automatic control system for the process water valve group, and optimizing parameters to achieve smooth drainage of the separator and maintain stable production in the hydrogen-based vertical furnace. The method is characterized by comprising the following steps:

[0027] S1. Install a direct cooling water valve group on the upper part of the process gas quenching orifice plate. High-pressure direct cooling water is sprayed into the airflow through the holes on the inner tube to cool the gas. A dosing device is installed on the direct cooling water supply main pipe. A certain proportion of dispersant solution is injected according to the direct cooling water usage to prevent the sedimentation and aggregation of solid particles in the direct cooling water system in the process gas loop, protect the pipeline from scale erosion, and reduce the blockage of the separator drainage system.

[0028] S2. Two tangential inlets for flushing water are set in the conical part of the process gas separator. A set of high-pressure direct cooling water valves including a shut-off valve YSV120401 and a flow regulating valve FV120401 are set. 10-20m3 / h of direct cooling water is injected tangentially to continuously flush the conical part of the process gas separator to prevent solids and sludge from settling and getting stuck on the bottom cone. The washed process gas and water are discharged from the lower pipe.

[0029] S3. Four interfaces are installed at the bottom of the process gas separator for liquid level transmitters, one for control and three for SIS safety system, namely LT120402 and LIT120401A / B / C. The container liquid level is controlled by valve LV120402A / B. There is a stop valve YSV120404 controlled by system interlock upstream. When the liquid level regulating valve LV120402A / B is put into use at the same time, LV120402A is the main valve and LV120402B is the auxiliary valve. The opening is adjusted according to the liquid level. At the same time, LV120402A / B is used as the auxiliary valve. The 2B auxiliary valve is designed with a timed valve opening control program. Every T hours, the drain valve LV120402B is opened to 100%. This increases the drainage flow rate to flush out sludge solids accumulated due to prolonged valve use and reduce clogging. T is optimized in the automatic control program based on data related to process direct cooling water, and the unit is hours. This parameter optimization automatically achieves smooth drainage of the separator, freeing manpower from the intense hydrogen-based shaft furnace smelting process while enhancing the stability of the shaft furnace smelting and achieving automated, clean, efficient, and stable production of hydrogen-based shaft furnace smelting.

[0030] S4. After entering automatic control, set the process gas separator control liquid level parameter LY120401. According to the actual liquid level LV120401 measured by the liquid level gauge at the bottom of the process gas separator during the vertical furnace smelting process, compare the size of LY120401 and LV120401. The automatic program control instruction directly adjusts the opening of the liquid level control valve LV120402A / B to achieve process gas separator liquid level adjustment. The adjustment principle is: when LV120401 is less than LY120401, reduce the opening of the control valve LV120402A / B to LV120401≈LY120401; when LV120401 is greater than LY120401, increase the opening of the control valve LV120402A / B to LV120401≈LV120401.

[0031] The determination principle of LV120401≈LY120401 is:

[0032] Let k = (LY120401-LV120401) / LY120401×100%. If the value of k is between -10% and 10%, it is determined that LV120401≈LY120401. When LV120401≈LY120401, the opening of the regulating valve LV120402A / B remains unchanged.

[0033] If the k value is not equal to -10% to 10%, adjust the opening of the liquid level control valve LV120402A / B, and adjust the valve position △h each time. After adjustment, maintain the time t, and then continue to determine the size relationship between LV120401 and LY120401 until the k value is between -10% and 10%;

[0034] Among them, △h is a parameter related to the valve position of the liquid level control valve LV120402A / B. The system selects that the unit of t is s, the unit of △h is %, and △h = 0.1%, t = 2S.

[0035] The electrical components that appear in this article are all electrical components that exist in reality.

[0036] Of course, the above description is not a limitation of the present invention, and the present invention is not limited to the above examples. Changes, modifications, additions or substitutions made by ordinary technicians in this technical field within the essential scope of the present invention also fall within the scope of protection of the present invention.

Claims

1. A method for preventing drainage and clogging of a hydrogen-based vertical furnace gas separator, comprising configuring a dispersant dosing device, setting a process water valve group, configuring an automatic control system for the process water valve group, and achieving smooth drainage of the separator through parameter optimization, characterized in that: The specific steps include: S1. Install a direct cooling water valve group on the upper part of the process gas quenching orifice plate. High-pressure direct cooling water is sprayed into the air flow through the holes on the inner tube. Install a dosing device on the direct cooling water supply main pipe. A certain proportion of dispersant solution is injected according to the direct cooling water usage to prevent the sedimentation and agglomeration of solid particles in the direct cooling water system in the process gas loop. S2, the conical part of the process gas separator is equipped with two tangential inlets for flushing water, and a set of high-pressure direct cooling water valves including a cut-off valve YSV120401 and a flow regulating valve FV120401 is set up. 3 / h of direct cooling water continuously flushes the conical part of the process gas separator to prevent solids and sludge from settling and getting stuck on the bottom cone. The washed process gas and water are discharged from the lower pipe; S3. Four interfaces for liquid level transmitters are installed at the bottom of the process gas separator: one for control and three for the SIS safety system, namely LT120402 and LIT120401A / B / C. The container liquid level is controlled by valve LV120402A / B. There is a stop valve YSV120404 upstream controlled by the system interlock. When the liquid level control valves LV120402A / B are put into use simultaneously, LV120402A serves as the main valve and LV120402B serves as the auxiliary valve, adjusting the opening according to the liquid level. At the same time, the LV120402B auxiliary valve is designed with a timed valve opening control program, which opens the drain valve LV120402B to 100% every T hours. This increases the drainage flow rate to flush the sludge solids accumulated due to long-term use of the valve. S4. After entering automatic control, set the process gas separator control liquid level parameter LY120401. According to the actual liquid level LV120401 measured by the liquid level gauge at the bottom of the process gas separator during the vertical furnace smelting process, compare the sizes of LY120401 and LV120401. The automatic program control instruction directly adjusts the opening of the liquid level control valve LV120402A / B to achieve process gas separator liquid level adjustment.

2. A method for preventing drainage and blocking of a hydrogen-based shaft furnace gas separator according to claim 1, characterized in that: In step S4, the adjustment principle is: when LV120401 is less than LY120401, the opening of the regulating valve LV120402A / B is reduced to LV120401≈LY120401; when LV120401 is greater than LY120401, the opening of the regulating valve LV120402A / B is increased to LV120401≈LY120401.

3. A method for preventing drainage and blocking of a hydrogen-based shaft furnace gas separator according to claim 2, characterized in that: In step S4, the determination principle of LV120401≈LY120401 is: Let k = (LY120401-LV120401) / LY120401×100%. If the k value is between -10% and 10%, it is determined that LV120401≈LY120401; when LV120401≈LY120401, the opening of the regulating valve LV120402A / B is kept unchanged.

4. A method for preventing drainage and blocking of a hydrogen-based shaft furnace gas separator according to claim 3, characterized in that: In step S4, if the k value is not equal to -10% to 10%, the opening of the liquid level control valve LV120402A / B is adjusted, and the valve position is adjusted by △h each time. After the adjustment, it is maintained for t time, and then the size relationship between LV120401 and LY120401 is continuously determined until the k value is between -10% and 10%; Among them, △h is a parameter related to the valve position of the liquid level control valve LV120402A / B. The system selects that the unit of t is s and the unit of △h is %.

5. The method for preventing drainage and blocking of a hydrogen-based vertical furnace gas separator according to claim 1, characterized in that: In step S3, T is optimized and set in the automatic control program according to data related to process direct cooling water, and the unit is h.

6. A method for preventing drainage and blocking of a hydrogen-based shaft furnace gas separator according to claim 4, characterized in that: In the step S4, Δh=0.1%, t=2S.

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