WO2019144523A1 - Multi-process flue gas purification system and method for controlling same - Google Patents

Multi-process flue gas purification system and method for controlling same Download PDF

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Publication number
WO2019144523A1
WO2019144523A1 PCT/CN2018/083579 CN2018083579W WO2019144523A1 WO 2019144523 A1 WO2019144523 A1 WO 2019144523A1 CN 2018083579 W CN2018083579 W CN 2018083579W WO 2019144523 A1 WO2019144523 A1 WO 2019144523A1
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activated carbon
flue gas
gas purification
flow rate
subsystem
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PCT/CN2018/083579
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French (fr)
Chinese (zh)
Inventor
叶恒棣
刘雁飞
魏进超
刘昌齐
傅旭明
杨本涛
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中冶长天国际工程有限责任公司
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Priority to MYPI2020002559A priority Critical patent/MY193803A/en
Priority to RU2020122728A priority patent/RU2762190C1/en
Priority to BR112020011458-8A priority patent/BR112020011458B1/en
Priority to KR1020207012434A priority patent/KR102343392B1/en
Publication of WO2019144523A1 publication Critical patent/WO2019144523A1/en
Priority to PH12020550665A priority patent/PH12020550665A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/08—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
    • B01D53/12—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents according to the "fluidised technique"
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/402—Dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/025—Other waste gases from metallurgy plants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40084—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by exchanging used adsorbents with fresh adsorbents
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)

Definitions

  • the present application relates to the field of gas purification technologies, and in particular, to a multi-process flue gas purification system and a control method thereof.
  • Iron and steel enterprises are the pillars of the entire national economy. However, while making important contributions to economic development, they are also accompanied by serious pollution problems.
  • smoke emissions such as sintering, pelletizing, coking, iron making, steel making and steel rolling.
  • the flue gas emitted in each process contains a large amount of dust, SO 2 and NO X. Contaminants. When polluted smoke is emitted into the atmosphere, it not only pollutes the environment, but also poses a threat to human health.
  • the flue gas purification device contains a material having an adsorption function (for example, activated carbon) to adsorb flue gas, so as to purify the flue gas discharged from each process.
  • adsorption function for example, activated carbon
  • the activated carbon flue gas purification technology of the existing steel enterprises is applied in the flue gas purification system, and the flue gas purification system includes the flue gas purifying device 1 installed in each process, and several activated carbon analytical activation subsystems 2, each of which is activated and deactivated by activated carbon.
  • the subsystems 2 are respectively in communication with each of the flue gas cleaning devices 1 via respective activated carbon delivery subsystems 3.
  • the activated carbon flue gas purification device 1 includes a feeding device 11 , an adsorption tower 12 , a discharging device 13 , a buffer silo 14 and a discharging device 15 ;
  • the activated carbon analytical activation subsystem 2 includes a buffer chamber 21 and a feeding material.
  • the activated carbon enters the adsorption tower 12 from the feeding device 11, and an activated carbon layer is formed in the adsorption tower 12.
  • the raw flue gas 17 containing the pollutants also continuously enters the adsorption tower 12, and the original flue gas 17 After the pollutants are adsorbed by the activated carbon in the adsorption tower 12, the clean flue gas 16 is discharged.
  • the contaminated activated carbon adsorbed with the pollutants is discharged to the buffer silo 14 through the discharging device 13, and discharged to the activated carbon conveying subsystem 3 by the discharging device 15 disposed under the buffer silo 14, and the activated carbon conveying subsystem 3
  • the contaminated activated carbon is transported to the buffer chamber 21 of the corresponding activated carbon analytical activation subsystem 2, and the contaminated activated carbon is released into the analytical tower 23 by the feeding device 22 disposed under the buffer chamber 21, and the clean activated carbon obtained by the analytical activation treatment is discharged.
  • Device 24 is discharged.
  • the activated carbon conveying subsystem 3 transports the clean activated carbon to the feeding device 11 of the corresponding flue gas purifying device 1, and enters the adsorption tower 12 again to purify the flue gas, thereby realizing the flue gas purifying device 1 and the activated carbon analytical activation subsystem 2
  • the flue gas purification treatment of one and the recycling of activated carbon is a flue gas purification treatment of one and the recycling of activated carbon.
  • each flue gas emission process in the iron and steel enterprise is provided with a set of flue gas purification device and a set of activated carbon analytical activation subsystem, and multiple flue gas purification devices and activated carbon analytical activation subsystem work simultaneously to achieve Purification of contaminated flue gas produced in each process.
  • different scale processes need to set up a scale-matched flue gas purification device, resulting in the flue gas set in the steel enterprise.
  • an independent activated carbon analytical activation subsystem is arranged, which leads to an excessive number of activated carbon analytical activation subsystems in the steel enterprise, which makes the overall structure of the flue gas purification system in the steel enterprise complex, and each process The generated flue gas is treated separately, resulting in a low efficiency of the flue gas purification system. Therefore, how to provide a flue gas purification system capable of efficiently treating flue gas has become an urgent problem to be solved in the art.
  • the present application provides a multi-process flue gas purification system and a control method thereof to solve the problem of low operating efficiency of the existing flue gas purification system.
  • the present application provides a multi-process flue gas purification system, comprising: an activated carbon centralized analytical activation subsystem, an activated carbon delivery subsystem, and a flue gas purification device corresponding to each process, and each of the flue gas purification devices respectively Connected to the activated carbon centralized analytical activation subsystem through the activated carbon transport subsystem;
  • the activated carbon centralized analytical activation subsystem comprises an analytical tower, a feeding device for controlling the flow rate of the contaminated activated carbon entering the analytical tower, and a discharging device for discharging the activated activated carbon in the analytical tower after the activation treatment, for the purpose of a screening device for screening activated activated carbon discharged from a discharge device for collecting activated activated carbon activated carbon obtained by the screening device, and providing an outlet end of the flue gas purification device corresponding to each process and a feeding device a total activated carbon cartridge between the total activated carbon cartridge for collecting the polluted activated carbon discharged from the flue gas purification device in each process, and a belt scale disposed between the total activated carbon cartridge and the feeding device, the belt scale being used for
  • the contaminated activated carbon in the total activated carbon storage tank is sent to the analytical tower, and a new activated carbon replenishing device is disposed above the total activated carbon storage tank, and the new activated carbon replenishing device is used to replenish the activated carbon in the total activated
  • the method further includes: a flue gas purification device corresponding to a sintering process of the activated carbon concentration analysis activation subsystem, and a material distribution device located below the activated activated carbon cartridge; and the flue gas purification device corresponding to the sintering process
  • the polluted activated carbon is sent to the analytical tower through the activated carbon conveying subsystem and the feeding device;
  • the materializing device includes a step n discharging device for distributing activated carbon for each step, and a sintering step discharging device for distributing activated carbon for the sintering step.
  • an embodiment of the present application provides a method for controlling a multi-process flue gas purification system, including the following steps:
  • the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t is determined;
  • the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the time t ni is determined according to the following steps:
  • W Sn(tni) is the total flow rate of SO 2 in the raw flue gas corresponding to the step n at time t ni , in units of kg/h
  • W Nn(tni) is the original flue gas corresponding to the step n at time t ni the total NO X flow rate, the unit kg / h
  • W Xn(tni) K 1 ⁇ W Sn(tni) + K 2 ⁇ W Nn(tni) ;
  • W Xn(tni) is the circulating flow rate of activated carbon at t ni time corresponding to the flue gas purification device in process n, unit kg/h; K 1 is the first coefficient, and the value ranges from 15 to 21; K 2 is the first The two coefficients are in the range of 3 to 5.
  • the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t is determined according to the following steps:
  • the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t is determined;
  • t is the current time
  • T ni is the time during which the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon concentration analysis activation subsystem.
  • the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t is determined according to the following steps:
  • the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n the supplementary flow rate W complement , and the following formula, determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
  • W X0 ⁇ W Xn(t-Tni)+ W complement .
  • the activated carbon loading amount Q 0 of the analytical tower in the activated carbon centralized analytical activation subsystem is determined;
  • Controlling said supplementary GAC GAC supplementary replenishing device activated charcoal loss quantity Q and complement loss quantity Q is equal to, activated carbon supplementary quantity Q adjusted up, new activated carbon per unit time determines supplementary device makeup flow W Make up .
  • the given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and the given frequency f p of the discharging device are adjusted according to the operating frequency f c of the belt weigher according to the following steps:
  • the relationship between the given frequency f g of the feeding device and the operating frequency f c of the belt weigher is obtained: Adjusting the given frequency f g of the feeding device according to the above formula and the operating frequency f c of the belt weigher;
  • the given frequency f p of the discharge device is adjusted according to the above formula and the operating frequency f c of the belt weigher.
  • an embodiment of the present application provides a method for controlling a multi-process flue gas purification system, including the following steps:
  • the activated carbon centralized analytical activation subsystem corresponding to the current time t is determined.
  • W X0 ⁇ W Xn(t-Tni)+ W X01 ;
  • it also includes:
  • the unloading flow rate W of the unloading device in the sintering process is determined to be unloaded ; wherein j is a coefficient, and the value is The range is from 0.9 to 0.97; and the discharge flow rate W of the unloading device of the process n is controlled to be the maximum.
  • an embodiment of the present application provides a method for controlling a multi-process flue gas purification system, including the following steps:
  • W X0 ⁇ W Xn(t-Tni)+ W complement + W X01 ;
  • the multi-process flue gas purification system and the control method thereof are provided by the embodiment of the invention, and the system comprises an activated carbon centralized analytical activation subsystem, an activated carbon conveying subsystem, and a flue gas purifying device corresponding to each process, and each flue gas purifying device
  • the activated carbon transport subsystem is connected with the activated carbon centralized analytical activation subsystem, and the polluted activated carbon discharged from the flue gas purification device corresponding to each process is respectively transported to the total activated carbon storage tank of the activated carbon centralized analytical activation subsystem, and then analyzed and activated by the analytical tower.
  • the activated activated carbon is then transported to the flue gas purification device of each process to realize the recycling of the activated carbon.
  • the process control unit provided in the flue gas purification device in each process sends the activated carbon circulating flow rate corresponding to the flue gas purifying device to the main control unit, and the main control unit uses the sum of the activated carbon circulating flow rates corresponding to all the processes to represent the activated carbon centralized analytical activation subsystem.
  • Activated carbon circulation flow and control the activation subsystem control unit set in the activated carbon concentration analysis activation subsystem to adjust the given frequency of the belt scale, feeding device and discharge device in the activated carbon centralized analytical activation subsystem, so that the activated carbon is concentrated analytically activated
  • the circulating flow rate of activated carbon at the subsystem is substantially equal to the sum of the circulating flow of activated carbon in the flue gas purification device in each process, so that the adsorption portion and the analytical portion of the multi-process flue gas purification system reach the purpose of synchronous operation, thereby enabling the activated carbon centralized analytical activation subsystem.
  • the theoretical activated carbon circulation flow rate is balanced with the activated carbon circulation flow rate of the flue gas purification device of each process to improve the operation efficiency.
  • FIG. 1 is a schematic structural view of a conventional flue gas purification system
  • FIG. 2 is a schematic structural view of a multi-process flue gas purification system according to Embodiment 1 of the present application;
  • FIG. 3 is a structural block diagram of a multi-process flue gas purification system according to Embodiment 1 of the present application;
  • FIG. 4 is a schematic structural view of a multi-process flue gas purification system according to Embodiment 2 of the present application;
  • FIG. 5 is a structural block diagram of a multi-process flue gas purification system according to Embodiment 2 of the present application.
  • FIG. 6 is a flowchart of a method for controlling a multi-process flue gas purification system according to an embodiment of the present application
  • FIG. 7 is a flow chart of a method for determining a circulating flow rate of activated carbon in a flue gas purification device in each process according to an embodiment of the present application;
  • FIG. 8 is a flow chart of a method for determining a supplementary flow rate for supplementing a new activated carbon according to an embodiment of the present application
  • FIG. 9 is a flowchart of a control method of a multi-process flue gas purification system according to still another embodiment of the present application.
  • FIG. 10 is a flow chart of a control method of a multi-process flue gas purification system provided by another embodiment of the present application.
  • 1-flue gas purification device 11-feeding equipment, 12-adsorption tower, 13-discharge equipment, 14-buffer silo, 15-discharge equipment, 16-net flue gas, 17-origin flue gas, 2-activated carbon concentration analysis activation subsystem, 21-buffer bin, 22-feeding device, 23-analysis tower, 24-discharge device, 25-total activated carbon bin, 26-belt scale, 27-screening device, 28- Activated activated carbon storage, 29-new activated carbon replenishing device, 20-separating device, 201-sintering process unloading device, 202-process unloading device, 3-activated carbon transport subsystem, 110-process 1 flue gas purification device, 111- Step 1 Feeding equipment, 112-Step 1 adsorption tower, 113-Step 1 discharge equipment, 114-Step 1 buffer silo, 115-Process 1 discharge equipment, 116-Process 1 net flue gas, 117-Process 1 original Flue
  • FIG. 2 is a schematic structural view of a multi-process flue gas purification system according to Embodiment 1 of the present application
  • FIG. 3 is a structural block diagram of a multi-process flue gas purification system according to Embodiment 1 of the present application.
  • a multi-process flue gas purification system provided by an embodiment of the present application includes: an activated carbon centralized analytical activation subsystem 2, an activated carbon delivery subsystem 3, and a flue gas purification device corresponding to each process, and each flue gas purification device.
  • the activated carbon delivery subsystem 3 is connected to the activated carbon centralized analytical activation subsystem 2, respectively.
  • a activated carbon centralized analytical activation subsystem 2 is disposed in the whole plant, and the flue gas purification devices provided at each process are respectively combined with the same activated carbon centralized analytical activation subsystem. 2 connected, that is, a one-to-many structural relationship is formed.
  • the multi-step flue gas purification system, the process 1 flue gas purification device 110, and the process 2 flue gas purification device 120 respectively have a tandem structure through the activated carbon transport subsystem 3 and the activated carbon centralized analytical activation subsystem 2,
  • the polluted activated carbon discharged from each flue gas purification device is separately transported to the activated carbon centralized analytical activation subsystem 2, and the activated activated carbon obtained after the analytical activation is separately transported to the flue gas purification device in each process to realize the circulation of the activated carbon. use.
  • FIG. 2 is merely an example showing the relationship between the step 1 flue gas purification device 110 and the step 2 flue gas purification device 120 and the activated carbon concentration analysis activation subsystem 2.
  • the multi-process flue gas purification system includes a plurality of flue gas purification devices corresponding to the processes.
  • only the multi-step flue gas purification system includes the step 1 flue gas purifying device 110 and the step 2 flue gas purifying device 120.
  • the method adopted is to transport by the activated carbon conveying subsystem 3. Because in the steel plant, the distance between two adjacent flue gas purification devices is far, and the activated carbon centralized analytical activation subsystem 2 and each flue gas purification device are in a series relationship, so that different flue gas purification devices and activated carbon are analyzed in a concentrated manner. The distance between the activation subsystems 2 is also different. In order to achieve efficient transportation and recycling of activated carbon, transportation by belt or conveyor may not be suitable for long distances.
  • the activated carbon conveying subsystem 3 in addition to the belt and the conveyor, can also be transported by using a car to avoid setting up a conveyor or a belt in the whole plant, increasing the floor space and affecting the structural layout of the whole plant. It can also increase the efficiency of the activated carbon transporting a long distance.
  • the activated carbon concentration analysis activation subsystem 2 includes an analysis tower 23 for analyzing and activating the polluted activated carbon discharged from the flue gas purification device corresponding to each process, so as to obtain activated activated carbon for recycling; and is disposed at the inlet end of the analytical tower 23.
  • the feeding device 22 is configured to send the total polluted activated carbon discharged from the flue gas purifying device corresponding to each step to the analytical tower 23 at a constant frequency or flow rate to accommodate the analytical activation frequency of the analytical tower 23;
  • the discharge device 24 at the outlet end, the discharge device 24 is connected to the inlet end of the flue gas purification device corresponding to each process through the activated carbon delivery subsystem 3, and the discharge device 24 is used to activate the activated carbon obtained by analytically activating the analytical column 23.
  • a certain frequency or flow rate is discharged into the activated carbon conveying subsystem 3, and then transported to the flue gas purifying device in each process; the total activated carbon storage chamber disposed between the outlet end of the flue gas purifying device corresponding to each process and the feeding device 25, for collecting polluted activated carbon discharged from the flue gas purification device in each process; and, being disposed in the total activated carbon cartridge 25 and the feedstock
  • a belt weigher 26 is disposed between 22 for transporting all contaminated activated carbon collected in the total activated carbon cartridge 25 to the activated carbon conveying subsystem 3, and then to the buffer tank 21 disposed above the feeding device 22, feeding
  • the device 22 effects communication between the buffer chamber 21 and the analytical column 23 to feed the contaminated activated carbon into the analytical column 23 at a constant flow rate or frequency through the feed device 22.
  • the flue gas purification device 110 of the first step includes a step 1 feeding device 111, a step 1 adsorption tower 112, a step 1 discharge device 113, a step 1 buffer silo 114, a step 1 discharge device 115, a process 1 activated carbon cartridge 118, and a process. 1 belt scale 119.
  • the activated carbon storage tank 118 of the process 1 is used to carry the activated activated carbon transported by the activated carbon centralized analytical activation subsystem 2, and is transported to the activated carbon conveying subsystem 3 through the belt scale 119 of the process 1, due to the purification of the flue gas.
  • the activated carbon conveying subsystem 3 may be a conveyor.
  • the activated activated carbon stored in the buffer chamber of the first step enters the adsorption tower 112 of the step 1 through the feed device 111 of the first step, and the raw flue gas 117 of the first step also enters the adsorption tower 112 of the first step, and the pollution carried by the raw flue gas 117 of the first step
  • the obtained step 1 net flue gas 116 is discharged.
  • the contaminated activated carbon adsorbed with the pollutants is discharged to the buffer silo 114 of the process 1 through the discharge device 113 of the process 1 for short-term storage.
  • the unloading device of the process 1 is processed.
  • the contaminated activated carbon is discharged into the activated carbon delivery subsystem 3.
  • the activated carbon conveying subsystem 3 may select an automobile, and then use the activated carbon conveying subsystem 3 to deliver the contaminated activated carbon into the total activated carbon cartridge 25, waiting for the analytical activation treatment.
  • the process 2 flue gas purification device 120 includes a process 2 feeding device 121, a process 2 adsorption tower 122, a process 2 discharge device 123, a process 2 buffer silo 124, a process 2 discharge device 125, and a process 2 activated carbon cartridge. 128 and step 2 belt scale 129 step 2.
  • Step 2 The flue gas purification device 120 performs the flue gas purification on the raw flue gas 117 in the step 2, and the process of obtaining the net flue gas 126 in the second step is the same as the flue gas purification device 110 in the first step, and will not be described herein.
  • the multi-process flue gas purification system provided in this embodiment further includes a computer subsystem 10, and the computer subsystem 10
  • the main control unit 100 is disposed, and the activation subsystem control unit 102 is disposed in the activated carbon concentration analysis activation subsystem for controlling the working state of each structure in the activated carbon centralized analysis activation subsystem 2 and adjusting the working parameters; and setting in each process
  • the process control unit in the middle flue gas purification device is configured to control the working state of each structure in the corresponding flue gas purifying device and adjust the working parameters;
  • the main control unit 100 is configured to perform bidirectional data with the activation subsystem control unit 102 and the process control unit.
  • control activation subsystem control unit 102 and the process control unit execute corresponding instructions, thereby achieving uniform and precise control of the entire multi-process flue gas purification system, and improving the operation efficiency of the flue gas purification.
  • the process control unit at each process has the following functions, that is, determining the activated carbon circulation flow W Xn(tni) corresponding to the flue gas purification device at the time t ni in the current process; and, in the current process
  • the process control unit at each process sends the activated carbon flow rate in the corresponding flue gas purification device to the main control unit 100, so that the main control unit 100 calculates and calculates the activated carbon flow rate of the flue gas purification device in all processes.
  • the analysis is to adjust the working state of the flue gas purification device in the corresponding process, so that the operating efficiency of the overall multi-process flue gas purification system is maximized.
  • the process control unit corresponding to the corresponding process n determines the activated carbon circulation flow W Xn(tni) corresponding to the flue gas purification device at the time t ni in the current process as follows:
  • step n generated in the production process of the original total amount of flue gas V n, according to the following formula and calculate the total SO 2 and NO X flow rate corresponding to the original flue t ni in time;
  • W Sn(tni) is the total flow rate of SO 2 in the raw flue gas corresponding to the step n at time t ni , in units of kg/h
  • W Nn(tni) is the original flue gas corresponding to the step n at time t ni the total NO X flow rate, the unit kg / h
  • V n is the total original flue t ni corresponding to the time, the unit Nm 3 / h
  • the flue gas purification device that mainly removes the flue gas NO X and sO 2, and therefore, can be estimated theoretically required according to the amount of sO 2 and NO X into the adsorption tower of the flue gas carried in The amount of activated carbon is used to achieve the best adsorption effect, and neither adsorption saturation nor insufficient adsorption occurs.
  • W Xn(tni) K 1 ⁇ W Sn(tni) + K 2 ⁇ W Nn(tni) ;
  • W Xn(tni) is the circulating flow rate of activated carbon at t ni time corresponding to the flue gas purification device in process n, unit kg/h; K 1 is the first coefficient, and the value ranges from 15 to 21; K 2 is the first The two coefficients are in the range of 3 to 5.
  • the flow state of the activated carbon and the flue gas are required.
  • flow state satisfies a certain proportional relationship, i.e., flue gas cleaning certain ratio between SO 2 and NO X flow rate total flow circulation apparatus charcoal original flue gas.
  • the process control unit at each process sends the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the current process to the main control unit 100, for example, the process 1 control unit 1011 converts the activated carbon of the process 1 flue gas purification device 110.
  • the circulation flow rate W X1 (t1i) is sent to the main control unit 100; the process 2 control unit 1012 transmits the activated carbon circulation flow rate W X2 (t2i) of the process 2 flue gas purification device 120 to the main control unit 100; the process n control unit 101n processes the process
  • the activated carbon circulation flow rate W Xn(tni) of the n flue gas purification device is sent to the main control unit 100.
  • the main control unit 100 acquires the activated carbon to the circulating flow rate W Xn (tni) t ni corresponding to the time step n, flue gas cleaning equipment, activated carbon in accordance with all the processes in the circulation flow rate W Xn (tni) flue gas purification device, determining a current time t
  • the corresponding activated carbon concentrates on the activated carbon circulation flow W X0 of the activation subsystem.
  • the circulation amount W X0 is the theoretical activated carbon circulation amount of the activated carbon centralized analytical activation subsystem, and the operating state and working parameters of the activated carbon centralized analytical activation subsystem can be accurately controlled according to the theoretical value.
  • the main control unit 100 determines, according to the following formula, the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t according to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n;
  • T ni is the time during which the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon concentration analysis activation subsystem at time i, and is provided by the activated carbon delivery subsystem 3.
  • the activated carbon circulation flow W X0 of the activated carbon centralized analysis activation subsystem is the sum of the activated carbon circulation flow rate of the flue gas purification device in each process, but the current time t when calculating the theoretical activated carbon circulation flow of the activation activated subsystem 2 in the activated carbon concentration is not
  • Each of the process control units determines the amount of activated carbon circulation of the flue gas purification device in each of the respective processes and the time t ni at which the data is transmitted.
  • the polluted activated carbon received in the activation subsystem 2 is just the polluted activated carbon discharged from the flue gas purification device in the corresponding process, that is, the circulating flow rate of the contaminated activated carbon received by the activated carbon concentration analysis activation subsystem 2 cannot be ensured as the activated carbon actually in the corresponding flue gas purification device.
  • the activated carbon circulation flow rate, and the current time t activates the activated carbon circulation flow obtained by the subsystem control unit 102
  • the corresponding process needs to be obtained after the transportation time T ni , that is, the precise control of the multi-process flue gas purification system needs to be extended. After the T ni period, this will reduce the operating efficiency, resulting in an inaccurate theoretical activated carbon circulation flow W X0 of the activated activated carbon concentration analysis activation subsystem.
  • the current time t when calculating the circulating flow rate of the activated carbon of the activated carbon concentration analysis activation subsystem 2 is 10:00, and the time T 1i of the polluted activated carbon discharged from the flue gas purification device in the process 1 to the activated carbon concentration analysis activation subsystem is 0.5.
  • the step 1011 the control unit 1 need to be 9.30 t 1i corresponding to the time step 1 charcoal circulation flow rate W X1 (t1i) flue gas cleaning apparatus 100 transmits to the main control unit;
  • active carbon concentration calculating analytical The current time t of the theoretical activated carbon circulation flow of the activation subsystem 2 is 14:20, and the time T 2i of the contaminated activated carbon discharged from the flue gas purification device in the process 2 to the activated carbon centralized analytical activation subsystem is 40 minutes, then, the process 2
  • the control unit 1012 transmits the activated carbon circulation flow rate W X2 (t2i) of the flue gas purification device in the step 2 corresponding to the time T 2i at 13:40 to the main control unit 100.
  • the accuracy of the activated carbon circulation flow W Xn(tni) of the flue gas purification device in each process in order to obtain the data. It can accurately represent the activated carbon circulating flow W X0 of the activation subsystem of the activated carbon concentration at the current time t. Therefore, it is necessary to acquire the activated carbon circulation of the flue gas purification device in each process corresponding to the time period of the transportation time T ni at the current time t.
  • the flow rate that is, the flow rate of the activated carbon circulation of the flue gas purification device in each step corresponding to the current time t is converted by W Xn(t-Tni) .
  • the main control unit 100 determines that the activated carbon concentrates on the activated carbon circulating flow W X0 of the activation subsystem, it is necessary to adjust the blanking flow rate of the belt scale 26 according to the data to adjust the feeding device of the analytical tower 23 according to the blanking flow rate of the belt scale 26 . 22 and the discharge flow rate of the discharge device 24, such that the discharge flow rate of the belt balance 26, the discharge flow rate of the feeding device 22, and the discharge flow rate of the discharge device 24, and the theoretical activated carbon cycle of the activated carbon concentration analysis activation subsystem 2
  • the flow rate is equal, achieving the effect of accurately controlling the multi-process flue gas purification system.
  • the activated carbon circulation flow rate of the flue gas purification device for each process can be the same as the activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem 2,
  • the whole multi-process flue gas purification system can realize synchronous operation, avoiding the amount of activated activated carbon transported by the activated carbon centralized analytical activation subsystem 2, which is insufficient to support the amount of adsorbed flue gas at the flue gas purification device in each process, and reduce the adsorption effect.
  • the amount of activated activated carbon transported by the activated carbon concentration analysis activation subsystem 2 is too large, so that the flue gas purification devices in each process are in a saturated state, and the activated activated carbon overflows. Therefore, it is necessary to control the blanking flow rate W C of the belt weigher 26 to be equal to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem.
  • the activation subsystem control unit 102 adjusts the blanking flow rate W C of the belt scale 26 according to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem, so that the blanking flow rate of the belt scale 26 is gradually combined with the activated carbon concentration analysis activation subsystem 2
  • the operating frequency f c is the operating frequency of the theoretical belt scale 26, i.e., step enables multiple operating frequency flue gas purification system to achieve synchronous operation.
  • the main control unit 100 then acquires the belt weigher 26 running frequency f c, the frequency f c of the operating belt scale 26, the sub control unit 102 transmits the activation instruction to adjust to the activated sub-system control unit 102 to adjust the feed apparatus 22 given frequency f g and discharge device 24 of a given frequency f p, in order to achieve control of multiple process flue gas purification system.
  • the main control unit 100 analyzes and calculates data according to the acquired data, and generates a control instruction according to the result to control the activation subsystem control unit 102 to perform corresponding operations. Therefore, exactly according to the operation frequency f c belt scale 26, adjusting the feed means to a predetermined frequency 22 f g and discharge device 24 for a given frequency f p, the main control unit 100 is configured to execute the following program steps:
  • Kc, K g and K p are constant, and are related to the width of the belt scale 26, the outlet width of the feeding device 22, the outlet width of the discharge device 24, the motor and the frequency converter parameters, and the specific gravity of the activated carbon.
  • the motor Since the belt scale 26, the feeding device 22, and the discharging device 24 are all feeding devices transported by the motor with animal materials, the motor is dragged by the frequency converter, and the running frequency of the frequency converter determines the rotation speed thereof, so that the belt scale 26 and the feeding device 22.
  • the material delivery flow rate of the discharge device 24 is proportional to the motor rotation speed, that is, the discharge flow rate is proportional to the rotation speed of the motor.
  • the circulation flow rate of the activated carbon for the flue gas purification device of each process can be the same as the circulation flow rate of the activated carbon of the activated carbon concentration analysis activation subsystem 2, so that the entire multi-process flue gas purification system can realize synchronous operation, and needs to be analyzed according to the activated carbon concentration.
  • the theoretical activated carbon circulation flow rate W X0 of the activation subsystem 2 adjusts the discharge flow rate of the belt scale 26, and then adjusts the discharge flow rate of the feeding device 22 and the discharge device 24 of the analytical tower 23 according to the discharge flow rate of the belt balance 26, so that the belt
  • the discharge flow rate W C of the scale 26, the discharge flow rate W G of the feed device 22, and the discharge flow rate W P of the discharge device 24 are equal to the theoretical activated carbon circulation flow rate W X0 of the activated carbon concentration analysis activation subsystem.
  • the proportional relationship between the given frequency f p of the discharging device 24 and the operating frequency f c of the belt scale 26, f g , f p can be adjusted to f c
  • the blanking flow rate W C of the belt scale 26, the blanking flow rate W G of the feeding device 22, and the blanking flow rate W P of the discharging device 24, and the activated carbon centralized analytical activation subsystem activated carbon is equal to the theoretical W X0 circulation flow, such that the theoretical activated charcoal concentrate circulation rate W X0 parsing subsystem activated charcoal and the circulation flow rate of the flue gas purification device in each step to reach equilibrium, so as to ensure the entire multi-step gas purification system to achieve synchronous operation , the operating efficiency is best.
  • the supplemental point of the new activated carbon is located in the activated carbon concentration analysis activation subsystem 2, that is, the activated carbon concentration analysis activation subsystem 2 provided in the embodiment further includes: a new activated carbon replenishing device 29 disposed above the total activated carbon cartridge 25.
  • the device supplementing the new activated carbon is disposed at the total activated carbon storage tank 25, because the total activated carbon cartridge 25 is used for receiving the polluted activated carbon discharged from the flue gas purification device in all processes of the whole plant, and is uniformly transported after receiving all the contaminated activated carbon.
  • the analytical activated carbon is analyzed and activated, and the activated activated carbon obtained is uniformly transported to the flue gas purification device of each step to realize the recycling of the activated carbon.
  • the total activated carbon cartridge 25 receives all the polluted activated carbon, and can accurately determine how much activated carbon is lost in the adsorption of flue gas and the transportation process of the activated carbon in the flue gas purification device in each process, and can be uniformly supplemented in the total activated carbon storage tank 25 To avoid the addition of activated carbon to the flue gas purification device in each process, it is not guaranteed that the amount of new activated carbon will be replenished each time, and the overall operating efficiency of the system will also be affected.
  • the new activated carbon replenishing device 29 is provided with a replenishing carbon control unit 104, which performs bidirectional data transmission with the main control unit 100, and the refueling control unit 104 is configured to control the new according to the instruction of the main control unit 100.
  • the activated carbon replenishing device 29 replenishes the new activated carbon cartridge 25 with new activated carbon at a certain frequency.
  • the main control unit 100 of the multi-process flue gas purification system determines the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t according to the following steps:
  • a fill control unit 104 determines a new carbon GAC supplementary replenishing device 29 is activated a new makeup flow W complement. Since the activated carbon centralized analytical activation subsystem 2 uniformly analyzes and activates all the polluted activated carbon, and the activated activated carbon is uniformly transported to each process, and the flue gas purification device is not provided with the screening loss carbon in each process, but is concentrated in the activated carbon. The activation subsystem 2 is analyzed to perform uniform screening of charcoal to ensure the accuracy of the data of the screened charcoal and improve the operating efficiency of the overall system.
  • the activated carbon concentration analysis activation subsystem 2 further includes: a screening device 27 located below the discharge device 24 and an activated activated carbon cartridge 28 located below the screening device 27, the screening device 27 being used for the parsing tower 23
  • the activated activated carbon is analyzed for sieving, and the activated activated carbon having the target particle size is obtained and stored in the activated activated carbon storage tank 28.
  • the activated activated carbon in the activated carbon storage tank 28 is the source of the activated carbon required for the flue gas purification device in each process.
  • the sieving device 27 may be a vibrating screen or other sieving device, which is not specifically limited in this embodiment.
  • the screening device 27 generates a small amount of loss when sieving the analyzed activated carbon, and the loss may include the loss of activated carbon caused by the flue gas purification device in the process of adsorbing the flue gas in the process.
  • the amount of new activated carbon needed to be replenished in the total activated carbon storage tank 25 can be accurately and quickly determined to ensure the theoretical activated carbon circulation flow W X0 of the activated carbon concentration analysis activation subsystem and the flue gas purification of each process.
  • the circulating flow rate of the activated carbon of the device is balanced, thereby ensuring that the entire multi-process flue gas purification system can realize synchronous operation and the operation efficiency is optimal.
  • the activation subsystem control unit 102 in this embodiment adopts the following method steps:
  • the amount of depleted activated carbon is determined by using the difference between the amount of all contaminated activated carbon entering the analytical column and the amount of activated activated carbon discharged.
  • Subsystem is activated by the control unit 102 detects the actual current time t activated activated carbon cartridge quantity Q corresponding to the solid, and then run in a multi-step cycle flue gas purification system loaded activated carbon 23 within the desorber quantity Q 0, can be determined according to At the time, all the lost activated carbon was produced.
  • new control quantity added activated charcoal with supplementary means loss of activated complement Q loss quantity Q is equal to, activated carbon supplementary quantity Q adjusted up, determining new activated charcoal add new supplementary device makeup flow per unit time W Make up .
  • the amount of depleted activated carbon produced by the screening device 27 is Q loss , which is the amount of new activated carbon to be actually replenished by the new activated carbon replenishing device 29.
  • the loss of activated carbon loss quantity Q as a reference the new device consists of activated complement new supplementary control unit 104 controls the carbon 29 according to the loss quantity Q activated charcoal added loss quantity Q is determined complement.
  • the supplementary flow W supplement of the new activated carbon per unit time can be determined.
  • W X0 ⁇ W Xn(t-Tni)+ W complement .
  • the total activated carbon storage tank 25 includes the polluted activated carbon discharged from the flue gas purification device in each process and the newly added new activated carbon
  • the above-mentioned activated carbon circulation flow rate should be comprehensively considered when determining the theoretical activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem 2.
  • Activated carbon concentrated analytical activation subsystem 2 generates carbon loss at the current cycle, and then supplements to ensure that the activated carbon concentrates on the activated carbon circulation flow corresponding to the activation subsystem in the next cycle, and the activated carbon circulation flow in the flue gas purification device in each process The sum is equal.
  • the present embodiment can improve the accuracy of the loss and the replenishing quantity by uniformly screening the carbon loss and uniformly supplementing the new activated carbon, and can minimize the time of the operation, thereby improving the multi-process flue gas purification system. operating efficiency.
  • the multi-process flue gas purification system provided by the embodiment of the present application includes the activated carbon centralized analytical activation subsystem 2, the activated carbon conveying subsystem 3, and the flue gas purification device corresponding to each process, and each flue gas purification device.
  • the device is respectively connected to the activated carbon centralized analytical activation subsystem 2 through the activated carbon conveying subsystem 3, and the polluted activated carbon discharged from the flue gas purification device corresponding to each process is respectively transported to the total activated carbon storage tank 25 of the activated carbon centralized analytical activation subsystem 2, and then the analytical tower 23
  • the analysis and activation are carried out, and the activated activated carbon obtained is transported to the flue gas purification device of each step to realize the recycling of the activated carbon.
  • the process control unit provided in the flue gas purification device in each step transmits the activated carbon circulation flow rate corresponding to the flue gas purification device to the main control unit 100, and the main control unit 100 uses the sum of the activated carbon circulation flow rates corresponding to all the processes to represent the active carbon concentration analysis activator.
  • the activated carbon of the system 2 circulates the flow rate, and controls the activation subsystem control unit 102 disposed in the activated carbon concentration analysis activation subsystem 2 to adjust the belt scale 26, the feeding device 22, and the discharge device 24 of the activated carbon concentration analysis activation subsystem 2.
  • the activated carbon circulating flow at the activated activated carbon system 2 is substantially equal to the total activated carbon circulating flow rate of the flue gas purification device in each process, so that the adsorption portion and the analytical portion of the multi-process flue gas purification system are synchronized.
  • the purpose is to make the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem and the activated carbon circulating flow of the flue gas purifying device of each process reach equilibrium, thereby improving the operating efficiency.
  • FIG. 4 is a schematic structural view of a multi-process flue gas purification system according to Embodiment 2 of the present application
  • FIG. 5 is a structural block diagram of a multi-process flue gas purification system according to Embodiment 2 of the present application.
  • the multi-process flue gas purification system provided in the second embodiment of the present application is different from the above embodiment in that the system can also be applied in a sintering process due to sintering in a steel plant.
  • the flue gas generated by the process is much larger than the flue gas produced by other processes, that is, the amount of flue gas generated in the sintering process is 70% of the total flue gas volume of the steel plant.
  • the sintering process is set up together with the activated carbon concentration analysis activation subsystem 2, that is, the multi-process flue gas purification system further includes a sintering process disposed in the activated carbon concentration analysis activation subsystem 2 Flue gas purification device.
  • the contaminated activated carbon discharged from the flue gas purification device 4 in the sintering process is not transported to the total activated carbon cartridge 25 for short-term storage, and can be directly sent to the analytical tower 23 for analytical activation.
  • the sintering process may include 1# sintering and 2# sintering.
  • two activated carbon concentrated analytical activators may be provided correspondingly.
  • System 2 In the present embodiment, only one activated carbon concentration analysis activation subsystem 2, one sintering process flue gas purification device 4, and a plurality of other process flue gas purification devices are exemplified.
  • the flue gas purification device 4 in the sintering process has the same structure as the flue gas purification device in each step shown in FIG. 2. Specifically, the flue gas purification device 4 in the sintering process includes a sintering process feeding device 41, a sintering process adsorption column 42 and Sintering process discharge device 43. In the sintering process, the flue gas purification device 4 performs the flue gas purification on the raw flue gas 44 in the sintering process to obtain the sintering process net flue gas 45.
  • the process is the same as the flue gas purification device 110 in the first step, and the corresponding process can refer to the content of the first embodiment. No longer.
  • the flue gas purification device 4 is provided with a sintering process control unit 103 for bidirectional data transmission with the main control unit 100, and controls the operation state of the flue gas purification device 4 in the sintering process according to the instruction of the main control unit 100. Adjust working parameters, etc.
  • the activated carbon circulating flow rate of the flue gas purification device 4 in the sintering process and the flue gas purification in each process are simultaneously considered.
  • the activated carbon circulation flow rate of the device When the sintering process is added in the multi-process flue gas purification system, when calculating the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis, the activated carbon circulating flow rate of the flue gas purification device 4 in the sintering process and the flue gas purification in each process are simultaneously considered.
  • the activated carbon circulation flow rate of the device when sintering process is added in the multi-process flue gas purification system, when calculating the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis, the activated carbon circulating flow rate of the flue gas purification device 4 in the sintering process and the flue gas purification in each process are simultaneously considered.
  • the activated carbon circulation flow rate of the device when sintering process is added in the multi-process flue gas pur
  • the sintering process control unit 103 determines the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process corresponding to the current time t, and to transmit the activated carbon circulation flow rate W X01 to the main control unit 100.
  • the sintering step is activated carbon gas purification apparatus of the circulation flow rate W X01 4, the above-described embodiments provide a method can be referred to, is determined according to SO 2 in the flue gas and the total flow rate of NO X, are not repeated herein.
  • the activated carbon circulation flow rate W X01 is transmitted to the main control unit 100, and the main control unit 100 determines the current time t according to the following steps.
  • the corresponding activated carbon concentrates on the activated carbon circulation flow W X0 of the activation subsystem:
  • the moment of the activated carbon circulation flow rate W X01 may be the current time t of calculating the activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem 2 .
  • W X0 ⁇ W Xn(t-Tni)+ W X01 .
  • the activated carbon circulating flow of the activated carbon concentration analysis is the sum of the activated carbon circulation flow rate of the flue gas purification device 4 in the sintering process and the activated carbon circulation flow rate of the flue gas purification device in each process, and if the multi-process flue gas purification is performed when the system is provided with activated carbon filters, and activated carbon new replenishment operation, in the calculation of focus activated charcoal activated parsing subsystem circulation rate, but also to consider the total active carbon cartridge 25 to add new makeup flow W complement activated carbon, activated carbon can ensure further The theoretical activated carbon circulation flow W X0 of the activation subsystem is concentrated and balanced with the sintering process and the activated carbon circulation flow of the flue gas purification device in each process, thereby ensuring that the entire multi-process flue gas purification system can realize synchronous operation and the operation efficiency is optimal.
  • the theoretical activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem changes, and the polluted activated carbon discharged from the flue gas purification device 4 in the sintering process is directly sent to the analytical tower 23, the total activated carbon Only the polluted activated carbon discharged from other processes is included in the bin 25.
  • the theoretical activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem 2 is the sum of the activated carbon circulation flow rate discharged by the flue gas purification device 4 in the sintering process and the activated carbon circulation flow rate of the flue gas purification device in other processes.
  • the activation subsystem control unit 102 is further configured to perform the following program steps: adjusting the belt scale according to the activated carbon circulation flow W X0 of the activated carbon concentration analysis activation activated carbon system and the activated carbon circulation flow rate W X01 of the flue gas purification apparatus in the sintering process
  • the given frequency f g of the feeding device 22 of the analytical tower 23 After the operating frequency f c of the belt scale 26 is re-determined, the given frequency f g of the feeding device 22 of the analytical tower 23, the given frequency f p of the discharging device 24 and the operating frequency f c of the belt scale 26 are again calculated.
  • the discharge flow rate W P of the G and the discharge device 24 is equal, so that the theoretical activated carbon circulation flow W X0 of the activated carbon centralized analysis activation subsystem and the activated carbon circulation flow rate of the flue gas purification device of each process are balanced, thereby ensuring the entire multi-process flue gas.
  • the purification system is capable of simultaneous operation and optimum operating efficiency.
  • the multi-process flue gas purification system provided in the embodiment includes the flue gas purifying device corresponding to the sintering process and the flue gas purifying device corresponding to the other processes, after the activated activated carbon is generated, there is a corresponding amount allocated for each process in the steel plant.
  • the problem with activated carbon is much larger than the amount of flue gas generated in the other processes. Therefore, in order to ensure the optimal adsorption effect of the flue gas purification device in the sintering process, it is necessary to allocate a large amount of activated activated carbon to the sintering process.
  • the amount of distribution needs to be determined according to the loading amount of the adsorption tower of the corresponding flue gas purification device or the circulating flow rate of the activated carbon corresponding to the sintering process, and the amount of activated carbon distributed to other processes is all the activated carbon remaining after being distributed to the sintering process.
  • the activated carbon concentration analysis activation subsystem 2 further includes a dispensing device 20 located below the activated activated carbon cartridge 28; the dispensing device 20 includes a process unloading device 202 for dispensing activated carbon for each process, and for In the sintering step, the unloading device 201 for activating the activated carbon is distributed.
  • the activated carbon is distributed to the flue gas purification device 4 in the sintering process in the steel plant by the sintering process unloading device 201, and the amount of activated carbon to be distributed is determined according to the loading amount of the adsorption tower in the corresponding flue gas purification device or the circulating flow rate of the activated carbon corresponding to the sintering process.
  • the amount of activated carbon dispensed in the sintering process is determined according to the loading amount of the adsorption column in the corresponding flue gas cleaning device.
  • Q- burning 0 is the loading amount of activated carbon in the adsorption tower in the sintering process, unit kg;
  • W X01 is the circulating flow rate of activated carbon at the current time t in the sintering process in the sintering process, unit kg/h;
  • T- burning is sintering activated carbon adsorption tower step the residence time in the range of 110 to 170, H units; wherein the residence time T 0 determined according to burn gas volume, gas velocity and the like.
  • the total discharge amount of the unloading device in the sintering process can be determined, and the discharge flow rate unloading of the unloading device 201 in the sintering process per unit time can be determined. 1 .
  • the amount of activated carbon dispensed in the sintering step is determined according to the circulating flow rate of activated carbon corresponding to the sintering step.
  • the coefficient of variation j of the weight that is, the discharge flow rate W of the unloading device 201 of the sintering process, is determined as follows:
  • W unload 1 W X01 ⁇ j
  • j is a coefficient, and the value ranges from 0.9 to 0.97.
  • the discharge flow rate of the discharging device 201 is, in fact, the discharge flow rate of each other unloading step W 2 concentration of the Theory of activated charcoal circulation flow rate W and the sintering step X0 discharge means activated subsystem 201 difference between the discharge flow rate W 1 discharged, but in order to ensure continuous operation of a multi-step flue gas purification system, and improve operational efficiency, in this embodiment, the step apparatus for dispensing the activated carbon each other flue gas cleaning process, the discharge device 202
  • the discharge flow W unloading 2 is set to the maximum to achieve the purpose of transporting how much material is stored in the material distribution device.
  • the new activated carbon replenishing device 29 can also be configured in the multi-process flue gas purification system provided in the second embodiment.
  • the main control unit 100 is configured to perform the following steps. To achieve precise control of multi-process flue gas purification systems:
  • W X0 ⁇ W Xn(t-Tni)+ W complement + W X01 ;
  • the multi-process flue gas purification system sets the sintering process for generating more flue gas together with the activated carbon centralized analytical activation subsystem, and the polluted activated carbon discharged from the flue gas purification device 4 in the sintering process can be at the fastest speed. Entering the activated carbon centralized analysis activation subsystem 2 for analytical activation, avoiding wasting time during transportation, resulting in reduced system operating efficiency. When the operating parameters of the activated carbon of the activation subsystem 2 are analyzed according to the activated carbon concentration, the circulation flow rate of the activated carbon corresponding to the sintering process and the circulating flow rate of the activated carbon corresponding to the other processes are fully considered, so that the feeding device for controlling the analytical tower is controlled.
  • the given frequency f g of 22, the given frequency f p of the discharge device 24 and the operating frequency f c of the belt scale 26 are equal, so as to ensure that the activated carbon concentrates on the activated carbon circulation flow W X0 and the sintering process. And the circulation flow rate of the activated carbon corresponding to the flue gas purification device corresponding to each process is balanced, thereby ensuring that the entire multi-process flue gas purification system can achieve synchronous and smooth operation, and the operation efficiency is optimal.
  • the embodiment of the present application provides a multi-process flue gas purification system control method, which is applied to the multi-process flue gas purification system provided by the above embodiment.
  • the control method includes the following steps:
  • the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the time t ni is determined according to the following steps:
  • step n generated in the production process of the original total amount of flue gas V n, and SO 2 and NO X in accordance with the total flow rate of the original flue t ni time corresponding to the following formula, is calculated;
  • W Sn(tni) is the total flow rate of SO 2 in the raw flue gas corresponding to the step n at time t ni , in units of kg/h
  • W Nn(tni) is the original flue gas corresponding to the step n at time t ni the total NO X flow rate, the unit kg / h
  • W Xn(tni) K 1 ⁇ W Sn(tni) + K 2 ⁇ W Nn(tni) ;
  • W Xn(tni) is the circulating flow rate of activated carbon at t ni time corresponding to the flue gas purification device in process n, unit kg/h; K 1 is the first coefficient, and the value ranges from 15 to 21; K 2 is the first The two coefficients are in the range of 3 to 5.
  • the step of determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t includes:
  • the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t is determined;
  • t is the current time
  • T ni is the time during which the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon concentration analysis activation subsystem.
  • the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t is determined according to the following steps:
  • the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n the supplementary flow rate W complement , and the following formula, determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
  • W X0 ⁇ W Xn(t-Tni) +W complement .
  • the activated carbon loading amount Q 0 of the analytical tower in the activated carbon centralized analytical activation subsystem is determined;
  • Controlling said supplementary GAC GAC supplementary replenishing device activated charcoal loss quantity Q and complement loss quantity Q is equal to, activated carbon supplementary quantity Q adjusted up, new activated carbon per unit time determines supplementary device makeup flow W Make up .
  • the given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and the given frequency f p of the discharging device are adjusted according to the operating frequency f c of the belt weigher according to the following steps:
  • the relationship between the given frequency f g of the feeding device and the operating frequency f c of the belt weigher is obtained: Adjusting the given frequency f g of the feeding device according to the above formula and the operating frequency f c of the belt weigher;
  • the given frequency f p of the discharge device is adjusted according to the above formula and the operating frequency f c of the belt weigher.
  • the embodiment of the present application provides a control method for a multi-process flue gas purification system, which is applied to the multi-process smoke provided by the above embodiment.
  • the gas purification system, the control method comprises the following steps:
  • W X0 ⁇ W Xn(t-Tni) +W X01 ;
  • it also includes:
  • the unloading flow rate W of the unloading device in the sintering process is determined to be unloaded ; wherein j is a coefficient, and the value is The range is from 0.9 to 0.97; and the discharge flow rate W of the unloading device of the process n is controlled to be the maximum.
  • the embodiment of the present application provides a multi-process flue gas purification system control method, which is applied to the multi-process smoke provided by the above embodiment.
  • the gas purification system, the control method comprises the following steps:
  • W X0 ⁇ W Xn(t-Tni)+ W complement + W X01 ;
  • the present invention further provides a computer storage medium, wherein the computer storage medium may store a program, where the program may be executed in the embodiments of the control method of the multi-process flue gas purification system provided by the present invention. Some or all of the steps.
  • the storage medium may be a magnetic disk, an optical disk, a read-only memory (English: read-only memory, abbreviated as: ROM) or a random access memory (English: random access memory, abbreviation: RAM).
  • the techniques in the embodiments of the present invention can be implemented by means of software plus a necessary general hardware platform. Based on such understanding, the technical solution in the embodiments of the present invention may be embodied in the form of a software product in essence or in the form of a software product, which may be stored in a storage medium such as a ROM/RAM. , a disk, an optical disk, etc., including instructions for causing a computer device (which may be a personal computer, server, or network device, etc.) to perform the methods described in various embodiments of the present invention or portions of the embodiments.
  • a computer device which may be a personal computer, server, or network device, etc.

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Abstract

A multi-process flue gas purification system and a method for controlling same. The flue gas purification system comprises an activated carbon centralized analysis activation subsystem (2), as well as flue gas purification devices (110, 120) corresponding to each process; each flue gas purification device (110, 120) is connected to the activated carbon centralized analysis activation subsystem (2) respectively by means of an activated carbon transport subsystem (3); a main control unit uses the sum of activated carbon circulating flows sent by corresponding process control units of all of the processes to represent the activated carbon circulating flow of the activated carbon centralized analysis activation subsystem (2), and controls an activation subsystem control unit (102) to adjust the given frequency of a beltweigher (26), a feeding device (22) and a discharging device (24) in the activated carbon centralized analysis activation subsystem (2) so that the sum of the activated carbon circulating flow at the activated carbon centralized analysis activation subsystem (2) and the activated carbon circulating flow of the flue gas purification device (110, 120) in each process is essentially equal.

Description

一种多工序烟气净化系统及其控制方法Multi-process flue gas purification system and control method thereof 技术领域Technical field
本申请涉及气体净化技术领域，尤其涉及一种多工序烟气净化系统及其控制方法。The present application relates to the field of gas purification technologies, and in particular, to a multi-process flue gas purification system and a control method thereof.
背景技术Background technique
钢铁企业是整个国民经济的支柱企业，但是，它为经济发展做出重要贡献的同时，也伴随着严重的污染大气的问题。钢铁企业内有很多工序都会产生烟气排放，例如，烧结、球团、炼焦、炼铁、炼钢和轧钢等工序，每个工序排放的烟气中含有大量的粉尘、SO 2和NO X等污染物。污染烟气被排放到大气中后，不仅污染环境，还会对人体健康构成威胁。为此，钢铁企业通常采用活性炭烟气净化技术，即在烟气净化装置中盛放具有吸附功能的物料(例如活性炭)吸附烟气，以实现对每个工序排放的烟气的净化处理。 Iron and steel enterprises are the pillars of the entire national economy. However, while making important contributions to economic development, they are also accompanied by serious pollution problems. There are many processes in the steel industry that generate smoke emissions, such as sintering, pelletizing, coking, iron making, steel making and steel rolling. The flue gas emitted in each process contains a large amount of dust, SO 2 and NO X. Contaminants. When polluted smoke is emitted into the atmosphere, it not only pollutes the environment, but also poses a threat to human health. For this reason, iron and steel enterprises usually adopt activated carbon flue gas purification technology, that is, the flue gas purification device contains a material having an adsorption function (for example, activated carbon) to adsorb flue gas, so as to purify the flue gas discharged from each process.
现有钢铁企业的活性炭烟气净化技术应用在烟气净化系统中，烟气净化系统包括设置在每个工序的烟气净化装置1，以及数个活性炭解析活化子系统2，每个活性炭解析活化子系统2分别通过相应的活性炭输送子系统3与每个烟气净化装置1对应连通。如图1所示，活性炭烟气净化装置1包括给料设备11、吸附塔12、排料设备13、缓冲料仓14和卸料设备15；活性炭解析活化子系统2包括缓冲仓21、给料装置22、解析塔23和排料装置24。系统运行时，活性炭由给料设备11进入吸附塔12中，在吸附塔12中形成活性炭料层，同时，含有污染物的原烟气17也源源不断地进入吸附塔12，原烟气17中的污染物经吸附塔12内的活性炭吸附后，得到洁净烟气16外排。而吸附有污染物的污染活性炭经过排料设备13排出到缓冲料仓14，再由设置在缓冲料仓14下方的卸料设备15排放到活性炭输送子系统3上，由活性炭输送子系统3将污染活性炭输送至对应的活性炭解析活化子系统2的缓冲仓21，污染活性炭再由设置在缓冲仓21下方的给料装置22释放进解析塔23内，通过解析活化处理得到的洁净活性炭由排料装置24排出。活性炭输送子系统3将洁净活性炭运送至对应的烟气净化装置1的给料设备11内，再次进入吸附塔12内进行烟气的净化，实现烟气净化装置1与活性炭解析活化子系统2一对一的烟气净化处理及活性炭的循环利用。The activated carbon flue gas purification technology of the existing steel enterprises is applied in the flue gas purification system, and the flue gas purification system includes the flue gas purifying device 1 installed in each process, and several activated carbon analytical activation subsystems 2, each of which is activated and deactivated by activated carbon. The subsystems 2 are respectively in communication with each of the flue gas cleaning devices 1 via respective activated carbon delivery subsystems 3. As shown in FIG. 1 , the activated carbon flue gas purification device 1 includes a feeding device 11 , an adsorption tower 12 , a discharging device 13 , a buffer silo 14 and a discharging device 15 ; the activated carbon analytical activation subsystem 2 includes a buffer chamber 21 and a feeding material. Device 22, analytical tower 23, and discharge device 24. When the system is in operation, the activated carbon enters the adsorption tower 12 from the feeding device 11, and an activated carbon layer is formed in the adsorption tower 12. At the same time, the raw flue gas 17 containing the pollutants also continuously enters the adsorption tower 12, and the original flue gas 17 After the pollutants are adsorbed by the activated carbon in the adsorption tower 12, the clean flue gas 16 is discharged. The contaminated activated carbon adsorbed with the pollutants is discharged to the buffer silo 14 through the discharging device 13, and discharged to the activated carbon conveying subsystem 3 by the discharging device 15 disposed under the buffer silo 14, and the activated carbon conveying subsystem 3 The contaminated activated carbon is transported to the buffer chamber 21 of the corresponding activated carbon analytical activation subsystem 2, and the contaminated activated carbon is released into the analytical tower 23 by the feeding device 22 disposed under the buffer chamber 21, and the clean activated carbon obtained by the analytical activation treatment is discharged. Device 24 is discharged. The activated carbon conveying subsystem 3 transports the clean activated carbon to the feeding device 11 of the corresponding flue gas purifying device 1, and enters the adsorption tower 12 again to purify the flue gas, thereby realizing the flue gas purifying device 1 and the activated carbon analytical activation subsystem 2 The flue gas purification treatment of one and the recycling of activated carbon.
在实际应用中，钢铁企业中的每个烟气排放工序均设置一套烟气净化装置和一套活性炭解析活化子系统，多个烟气净化装置和活性炭解析活化子系统同时工 作，以实现对每个工序产生的污染烟气的净化处理。然而，由于钢铁企业每个工序的规模以及产生的烟气量不同，为了实现最佳的烟气净化效果，不同规模的工序需要设置规模匹配的烟气净化装置，导致钢铁企业内设置的烟气净化装置的种类较多，无法进行统一管理。而为每个烟气净化装置分别配置独立的活性炭解析活化子系统，导致钢铁企业内活性炭解析活化子系统的设置数量过多，使得钢铁企业内烟气净化系统的整体结构复杂，且每一工序产生的烟气被单独处理，导致烟气净化系统的运行效率低。因此，如何提供一种能够高效处理烟气的烟气净化系统成为本领域亟待解决的问题。In practical application, each flue gas emission process in the iron and steel enterprise is provided with a set of flue gas purification device and a set of activated carbon analytical activation subsystem, and multiple flue gas purification devices and activated carbon analytical activation subsystem work simultaneously to achieve Purification of contaminated flue gas produced in each process. However, due to the scale of each process and the amount of smoke generated by the steel company, in order to achieve the best flue gas purification effect, different scale processes need to set up a scale-matched flue gas purification device, resulting in the flue gas set in the steel enterprise. There are many types of purification devices, and it is impossible to perform unified management. For each flue gas purification device, an independent activated carbon analytical activation subsystem is arranged, which leads to an excessive number of activated carbon analytical activation subsystems in the steel enterprise, which makes the overall structure of the flue gas purification system in the steel enterprise complex, and each process The generated flue gas is treated separately, resulting in a low efficiency of the flue gas purification system. Therefore, how to provide a flue gas purification system capable of efficiently treating flue gas has become an urgent problem to be solved in the art.
发明内容Summary of the invention
本申请提供了一种多工序烟气净化系统及其控制方法，以解决现有的烟气净化系统运行效率低的问题。The present application provides a multi-process flue gas purification system and a control method thereof to solve the problem of low operating efficiency of the existing flue gas purification system.
第一方面，本申请提供一种多工序烟气净化系统，包括：活性炭集中解析活化子系统，活性炭输送子系统，以及与各工序对应的烟气净化装置，每一所述烟气净化装置分别通过活性炭输送子系统与活性炭集中解析活化子系统连接；其中，In a first aspect, the present application provides a multi-process flue gas purification system, comprising: an activated carbon centralized analytical activation subsystem, an activated carbon delivery subsystem, and a flue gas purification device corresponding to each process, and each of the flue gas purification devices respectively Connected to the activated carbon centralized analytical activation subsystem through the activated carbon transport subsystem;
所述活性炭集中解析活化子系统包括解析塔，用于控制进入解析塔内污染活性炭流量的给料装置，用于将解析塔内经过活化处理后的活化活性炭排出的排料装置，用于对所述排料装置排出的活化活性炭进行筛分的筛分装置，用于收集经筛分装置后得到的活化活性炭的活化活性炭仓，设置在各工序对应的烟气净化装置的出口端与给料装置之间的总活性炭仓，所述总活性炭仓用于收集各工序中烟气净化装置排放的污染活性炭，设置在所述总活性炭仓与给料装置之间的皮带秤，所述皮带秤用于将总活性炭仓内的污染活性炭输送至解析塔，以及，设置在总活性炭仓上方的新活性炭补充装置，所述新活性炭补充装置用于向总活性炭仓内补充新活性炭。The activated carbon centralized analytical activation subsystem comprises an analytical tower, a feeding device for controlling the flow rate of the contaminated activated carbon entering the analytical tower, and a discharging device for discharging the activated activated carbon in the analytical tower after the activation treatment, for the purpose of a screening device for screening activated activated carbon discharged from a discharge device for collecting activated activated carbon activated carbon obtained by the screening device, and providing an outlet end of the flue gas purification device corresponding to each process and a feeding device a total activated carbon cartridge between the total activated carbon cartridge for collecting the polluted activated carbon discharged from the flue gas purification device in each process, and a belt scale disposed between the total activated carbon cartridge and the feeding device, the belt scale being used for The contaminated activated carbon in the total activated carbon storage tank is sent to the analytical tower, and a new activated carbon replenishing device is disposed above the total activated carbon storage tank, and the new activated carbon replenishing device is used to replenish the activated carbon in the total activated carbon storage tank.
可选地，还包括：设置于所述活性炭集中解析活化子系统的烧结工序对应的烟气净化装置，以及，位于活化活性炭仓下方的分料装置；所述烧结工序对应的烟气净化装置排放的污染活性炭通过活性炭输送子系统以及给料装置送入解析塔；Optionally, the method further includes: a flue gas purification device corresponding to a sintering process of the activated carbon concentration analysis activation subsystem, and a material distribution device located below the activated activated carbon cartridge; and the flue gas purification device corresponding to the sintering process The polluted activated carbon is sent to the analytical tower through the activated carbon conveying subsystem and the feeding device;
所述分料装置包括用于为各工序分配活化活性炭的工序n卸料装置，以及用于为烧结工序分配活化活性炭的烧结工序卸料装置。The materializing device includes a step n discharging device for distributing activated carbon for each step, and a sintering step discharging device for distributing activated carbon for the sintering step.
第二方面，本申请实施例提供一种多工序烟气净化系统的控制方法，包括以下步骤：In a second aspect, an embodiment of the present application provides a method for controlling a multi-process flue gas purification system, including the following steps:
确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)；其中， n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间； The activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the time t ni is determined; wherein n is the serial number of each step in the multi-process flue gas purification system; t ni =tT ni , T ni is the process n The time when the polluted activated carbon corresponding to the middle flue gas purification device is transported to the activated carbon concentration analysis activation subsystem at time i;
根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； According to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n, the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t is determined;
根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0时对应的所述皮带秤的运行频率f c； Adjusting the blanking flow rate W C of the belt scale according to the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem; and obtaining the operating frequency f c of the belt scale corresponding to W C = W X0 ;
根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 Adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize the multi-process flue gas purification system control.
可选地，按照下述步骤确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)： Optionally, the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the time t ni is determined according to the following steps:
根据工序n在生产过程中产生的原烟气总量V n，以及根据下式，计算t ni时刻对应的所述原烟气中的SO 2和NO X总流量； The step n generated in the production process of the original total amount of flue gas V n, and SO 2 and NO X in accordance with the total flow rate of the original flue t ni time corresponding to the following formula, is calculated;
W Sn(tni)＝V n×C Sn/10 6； W Sn(tni) = V n × C Sn /10 6 ;
W Nn(tni)＝V n×C Nn/10 6； W Nn(tni) = V n × C Nn /10 6 ;
式中，W Sn(tni)为工序n在t ni时刻对应的原烟气中的SO 2总流量，单位kg/h；W Nn(tni)为工序n在t ni时刻对应的原烟气中的NO X总流量，单位kg/h；C Sn为工序n在t ni时刻对应的原烟气中的SO 2浓度，单位mg/Nm 3；C Nn为工序n在t ni时刻对应的原烟气中的NO X浓度，单位mg/Nm 3； Where W Sn(tni) is the total flow rate of SO 2 in the raw flue gas corresponding to the step n at time t ni , in units of kg/h; W Nn(tni) is the original flue gas corresponding to the step n at time t ni the total NO X flow rate, the unit kg / h; 2 C Sn concentration of SO original flue step n at time t ni corresponding to the units mg / Nm 3; C Nn to step n at time t ni corresponding raw tobacco NO X in the gas concentration, the unit mg / Nm 3;
根据所述原烟气中的SO 2和NO X总流量，以及下式，计算t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)； The SO 2 X and the total flow of the raw flue gas NO, and the following equation, calculated t ni corresponding to the time step n flue gas purification device activated circulation flow rate W Xn (tni);
W Xn(tni)＝K 1×W Sn(tni)+K 2×W Nn(tni)； W Xn(tni) = K 1 × W Sn(tni) + K 2 × W Nn(tni) ;
式中，W Xn(tni)为工序n中烟气净化装置对应的t ni时刻的活性炭循环流量，单位kg/h；K 1为第一系数，取值范围为15～21；K 2为第二系数，取值范围为3～5。 In the formula, W Xn(tni) is the circulating flow rate of activated carbon at t ni time corresponding to the flue gas purification device in process n, unit kg/h; K 1 is the first coefficient, and the value ranges from 15 to 21; K 2 is the first The two coefficients are in the range of 3 to 5.
可选地，按照下述步骤确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0： Optionally, the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t is determined according to the following steps:
按照下式，根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； According to the following formula, according to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n, the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t is determined;
W X0＝∑W Xn(tni)＝∑W Xn(t-Tni)； W X0 = ∑W Xn(tni)= ∑W Xn(t-Tni) ;
式中，t为当前时刻，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间。 In the formula, t is the current time, and T ni is the time during which the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon concentration analysis activation subsystem.
可选地，按照下述步骤确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0： Optionally, the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t is determined according to the following steps:
确定新活性炭补充装置的补充新活性炭的补充流量W 补，以根据所述补充流量W 补，控制所述新活性炭补充装置向总活性炭仓内补充新活性炭； Determining supplementary replenishing device GAC GAC supplemental traffic complement of W, W to fill in accordance with the makeup flow, the control GAC GAC supply apparatus into the total activated carbon cartridge;
根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)，补充流量W 补，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； According to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n, the supplementary flow rate W complement , and the following formula, determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
W X0＝∑W Xn(t-Tni)+W 补。 W X0 = ∑W Xn(t-Tni)+ W complement .
可选地，按照下述步骤确定新活性炭补充装置的补充新活性炭的补充流量W 补： Alternatively, according to the following step of determining supplementary replenishing apparatus GAC GAC supplementary flow rate W Complement:
根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，按照下式，确定活性炭集中解析活化子系统中解析塔的活性炭装填料量Q 0； According to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem, according to the following formula, the activated carbon loading amount Q 0 of the analytical tower in the activated carbon centralized analytical activation subsystem is determined;
Q 0＝W X0×T 0； Q 0 = W X0 × T 0 ;
式中，Q 0为活性炭集中解析活化子系统中解析塔的活性炭装填料量，单位kg；T 0为解析塔内活性炭的停留时间，取值范围4～8，单位h； Wherein, Q 0 is the activated carbon loading amount of the analytical tower in the activated carbon concentration analysis activation subsystem, unit kg; T 0 is the residence time of the activated carbon in the analytical tower, the value ranges from 4 to 8, unit h;
检测所述活性炭集中解析活化子系统中活化活性炭仓的实际活性炭料量Q 实； Detecting the actual charcoal activated charcoal concentrated parsing subsystem quantity Q of the solid activated carbon cartridge;
根据所述解析塔的活性炭装填料量Q 0和实际活性炭料量Q 实，按照式Q 损＝Q 0-Q 实，确定活性炭经所述筛分装置筛分处理后的损耗活性炭料量Q 损； According to the analysis of activated carbon packed column quantity Q 0 of the activated carbon and the actual real quantity Q, in accordance with the formula Q = Q 0 -Q real loss, determine the loss quantity Q activated charcoal loss after sieving through the sieve processing means ;
控制所述新活性炭补充装置的补充活性炭料量Q 补与损耗活性炭料量Q 损相等，根据调整后的补充活性炭料量Q 补，确定单位时间的新活性炭补充装置的补充新活性炭的补充流量W 补。 Controlling said supplementary GAC GAC supplementary replenishing device activated charcoal loss quantity Q and complement loss quantity Q is equal to, activated carbon supplementary quantity Q adjusted up, new activated carbon per unit time determines supplementary device makeup flow W Make up .
可选地，按照下述步骤根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p： Optionally, the given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and the given frequency f p of the discharging device are adjusted according to the operating frequency f c of the belt weigher according to the following steps:
确定所述皮带秤的下料流量W C＝K c×f c，给料装置的下料流量W G＝K g×f g，排料装置的下料流量W P＝K p×f p；式中，Kc、K g和K p均为常数； Determining the discharge flow rate of the belt weigher W C = K c × f c , the discharge flow rate of the feeding device W G = K g × f g , the discharge flow rate of the discharge device W P = K p × f p ; Where Kc, K g and K p are constants;
控制所述活性炭集中解析活化子系统的给料装置、排料装置和皮带秤的下料流量相同，使得W G＝W P＝W C＝W X0； The feeding flow rate of the feeding device, the discharging device and the belt weigher for controlling the activated carbon centralized analytical activation subsystem is the same, so that W G = W P = W C = W X0 ;
根据上式，得到所述给料装置的给定频率f g与皮带秤的运行频率f c之间满足下式关系：
Figure PCTCN2018083579-appb-000001
以根据上式及皮带秤的运行频率f c，调整给料装置的给定频 率f g；以及， According to the above formula, the relationship between the given frequency f g of the feeding device and the operating frequency f c of the belt weigher is obtained:
Figure PCTCN2018083579-appb-000001
Adjusting the given frequency f g of the feeding device according to the above formula and the operating frequency f c of the belt weigher;
得到所述排料装置的给定频率f p与皮带秤的运行频率f c之间满足下式关系：
Figure PCTCN2018083579-appb-000002
以根据上式及皮带秤的运行频率f c，调整排料装置的给定频率f p。 Obtaining the following relationship between the given frequency f p of the discharge device and the operating frequency f c of the belt scale:
Figure PCTCN2018083579-appb-000002
The given frequency f p of the discharge device is adjusted according to the above formula and the operating frequency f c of the belt weigher.
第三方面，本申请实施例提供一种多工序烟气净化系统的控制方法，包括以下步骤：In a third aspect, an embodiment of the present application provides a method for controlling a multi-process flue gas purification system, including the following steps:
确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量W X01；以及，确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间； Determining the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process corresponding to the current time t; and determining the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the t ni time; wherein n is more The serial number of each process in the process flue gas purification system; t ni = tT ni , T ni is the time when the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon centralized analytical activation subsystem at time i;
根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)和烧结工序中烟气净化装置的活性炭循环流量W X01，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； According to the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n and the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process, and the following formula, the activated carbon centralized analytical activation subsystem corresponding to the current time t is determined. Activated carbon circulation flow W X0 ;
W X0＝∑W Xn(t-Tni)+W X01； W X0 = ∑W Xn(t-Tni)+ W X01 ;
根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0-W X01时对应的所述皮带秤的运行频率f c； Adjusting the discharge flow rate W C of the belt scale according to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem; and obtaining the operating frequency f c of the belt scale corresponding to W C = W X0 - W X01 ;
根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 Adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize the multi-process flue gas purification system control.
可选地，还包括：Optionally, it also includes:
根据所述烧结工序中烟气净化装置的活性炭循环流量W X01，以及式W 卸1＝W X01×j，确定烧结工序卸料装置的卸料流量W 卸1；其中，j为系数，取值范围为0.9～0.97；以及，控制所述工序n卸料装置的卸料流量W 卸2为最大。 According to the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process, and the formula W unloading 1 = W X01 × j, the unloading flow rate W of the unloading device in the sintering process is determined to be unloaded ; wherein j is a coefficient, and the value is The range is from 0.9 to 0.97; and the discharge flow rate W of the unloading device of the process n is controlled to be the maximum.
第四方面，本申请实施例提供一种多工序烟气净化系统的控制方法，包括以下步骤：In a fourth aspect, an embodiment of the present application provides a method for controlling a multi-process flue gas purification system, including the following steps:
确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量W X01，确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)；以及，确定新活性炭补充装置的补充新活性炭的补充流量W 补；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间； Determining the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process corresponding to the current time t, determining the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the time t ni ; and determining the new activated carbon replenishing device the activated carbon add new makeup flow up W; where, n is a multi-step gas purification system number of each step; t ni = tT ni, T ni flue gas purifying apparatus corresponding to the time step n contaminated activated carbon in the i transport The time until the activated carbon concentrates on the activation subsystem;
根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)、烧结工序中烟气 净化装置的活性炭循环流量W X01和补充流量W 补，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； The activated carbon circulation flow W Xn (tni) n in the step of the flue gas purification device, the sintering step of the activated carbon and the circulation flow rate supplemental flow rate W W X01 complement flue gas purification device, and the following equation, corresponding to the current time t is determined charcoal Concentrate analysis of activated carbon circulation flow W X0 of the activation subsystem;
W X0＝∑W Xn(t-Tni)+W 补+W X01； W X0 = ∑W Xn(t-Tni)+ W complement + W X01 ;
根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0-W X01时对应的所述皮带秤的运行频率f c； Adjusting the discharge flow rate W C of the belt scale according to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem; and obtaining the operating frequency f c of the belt scale corresponding to W C = W X0 - W X01 ;
根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 Adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize the multi-process flue gas purification system control.
采用本发明实施例提供的多工序烟气净化系统及其控制方法，该系统包括活性炭集中解析活化子系统，活性炭输送子系统，以及与各工序对应的烟气净化装置，每一烟气净化装置分别通过活性炭输送子系统与活性炭集中解析活化子系统连接，各工序对应的烟气净化装置排放的污染活性炭分别运送至活性炭集中解析活化子系统的总活性炭仓，再由解析塔进行解析活化，得到的活化活性炭再被运送至各工序的烟气净化装置，实现活性炭的循环利用。各工序中烟气净化装置内设置的工序控制单元将对应烟气净化装置的活性炭循环流量发送至主控制单元，主控制单元利用所有工序对应的活性炭循环流量的总和代表活性炭集中解析活化子系统的活性炭循环流量，并控制设置在活性炭集中解析活化子系统的活化子系统控制单元，以调整活性炭集中解析活化子系统中皮带秤、给料装置和排料装置的给定频率，使得活性炭集中解析活化子系统处的活性炭循环流量与各工序中烟气净化装置的活性炭循环流量总和实质相等，使得多工序烟气净化系统的吸附部分与解析部分达到同步运行的目的，进而使得活性炭集中解析活化子系统的理论活性炭循环流量与各工序的烟气净化装置的活性炭循环流量达到平衡，提高运行效率。The multi-process flue gas purification system and the control method thereof are provided by the embodiment of the invention, and the system comprises an activated carbon centralized analytical activation subsystem, an activated carbon conveying subsystem, and a flue gas purifying device corresponding to each process, and each flue gas purifying device The activated carbon transport subsystem is connected with the activated carbon centralized analytical activation subsystem, and the polluted activated carbon discharged from the flue gas purification device corresponding to each process is respectively transported to the total activated carbon storage tank of the activated carbon centralized analytical activation subsystem, and then analyzed and activated by the analytical tower. The activated activated carbon is then transported to the flue gas purification device of each process to realize the recycling of the activated carbon. The process control unit provided in the flue gas purification device in each process sends the activated carbon circulating flow rate corresponding to the flue gas purifying device to the main control unit, and the main control unit uses the sum of the activated carbon circulating flow rates corresponding to all the processes to represent the activated carbon centralized analytical activation subsystem. Activated carbon circulation flow, and control the activation subsystem control unit set in the activated carbon concentration analysis activation subsystem to adjust the given frequency of the belt scale, feeding device and discharge device in the activated carbon centralized analytical activation subsystem, so that the activated carbon is concentrated analytically activated The circulating flow rate of activated carbon at the subsystem is substantially equal to the sum of the circulating flow of activated carbon in the flue gas purification device in each process, so that the adsorption portion and the analytical portion of the multi-process flue gas purification system reach the purpose of synchronous operation, thereby enabling the activated carbon centralized analytical activation subsystem. The theoretical activated carbon circulation flow rate is balanced with the activated carbon circulation flow rate of the flue gas purification device of each process to improve the operation efficiency.
附图说明DRAWINGS
为了更清楚地说明本申请的技术方案，下面将对实施例中所需要使用的附图作简单地介绍，显而易见地，对于本领域普通技术人员而言，在不付出创造性劳动性的前提下，还可以根据这些附图获得其他的附图。In order to more clearly illustrate the technical solutions of the present application, the drawings used in the embodiments will be briefly described below. Obviously, for those skilled in the art, without any creative labor, Other drawings can also be obtained from these figures.
图1为现有的烟气净化系统的结构示意图；1 is a schematic structural view of a conventional flue gas purification system;
图2为本申请实施例一提供的多工序烟气净化系统的结构示意图；2 is a schematic structural view of a multi-process flue gas purification system according to Embodiment 1 of the present application;
图3为本申请实施例一提供的多工序烟气净化系统的结构框图；3 is a structural block diagram of a multi-process flue gas purification system according to Embodiment 1 of the present application;
图4为本申请实施例二提供的多工序烟气净化系统的结构示意图；4 is a schematic structural view of a multi-process flue gas purification system according to Embodiment 2 of the present application;
图5为本申请实施例二提供的多工序烟气净化系统的结构框图；5 is a structural block diagram of a multi-process flue gas purification system according to Embodiment 2 of the present application;
图6为本申请实施例提供的多工序烟气净化系统的控制方法的流程图；6 is a flowchart of a method for controlling a multi-process flue gas purification system according to an embodiment of the present application;
图7为本申请实施例提供的确定各工序中烟气净化装置的活性炭循环流量方法的流程图；7 is a flow chart of a method for determining a circulating flow rate of activated carbon in a flue gas purification device in each process according to an embodiment of the present application;
图8为本申请实施例提供的确定补充新活性炭的补充流量方法的流程图；8 is a flow chart of a method for determining a supplementary flow rate for supplementing a new activated carbon according to an embodiment of the present application;
图9为本申请又一实施例提供的多工序烟气净化系统的控制方法的流程图；9 is a flowchart of a control method of a multi-process flue gas purification system according to still another embodiment of the present application;
图10本申请另一实施例提供的多工序烟气净化系统的控制方法的流程图。FIG. 10 is a flow chart of a control method of a multi-process flue gas purification system provided by another embodiment of the present application.
图示说明：Illustration:
其中，1-烟气净化装置，11-给料设备，12-吸附塔，13-排料设备，14-缓冲料仓，15-卸料设备，16-净烟气，17-原烟气，2-活性炭集中解析活化子系统，21-缓冲仓，22-给料装置，23-解析塔，24-排料装置，25-总活性炭仓，26-皮带秤，27-筛分装置，28-活化活性炭仓，29-新活性炭补充装置，20-分料装置，201-烧结工序卸料装置，202-工序卸料装置，3-活性炭输送子系统，110-工序1烟气净化装置，111-工序1给料设备，112-工序1吸附塔，113-工序1排料设备，114-工序1缓冲料仓，115-工序1卸料设备，116-工序1净烟气，117-工序1原烟气，118-工序1活性炭仓，119-工序1皮带秤，120-工序2烟气净化装置，121-工序2给料设备，122-工序2吸附塔，123-工序2排料设备，124-工序2缓冲料仓，125-工序2卸料设备，126-工序2净烟气，127-工序2原烟气，128-工序2活性炭仓，129-工序2皮带秤，10-计算机子系统，100-主控制单元，1011-工序1控制单元，101n-工序n控制单元，102-活化子系统控制单元，103-烧结工序控制单元，104-补新炭控制单元，4-烧结工序中烟气净化装置，41-烧结工序给料设备，42-烧结工序吸附塔，43-烧结工序排料设备，44-烧结工序原烟气，45-烧结工序净烟气。Among them, 1-flue gas purification device, 11-feeding equipment, 12-adsorption tower, 13-discharge equipment, 14-buffer silo, 15-discharge equipment, 16-net flue gas, 17-origin flue gas, 2-activated carbon concentration analysis activation subsystem, 21-buffer bin, 22-feeding device, 23-analysis tower, 24-discharge device, 25-total activated carbon bin, 26-belt scale, 27-screening device, 28- Activated activated carbon storage, 29-new activated carbon replenishing device, 20-separating device, 201-sintering process unloading device, 202-process unloading device, 3-activated carbon transport subsystem, 110-process 1 flue gas purification device, 111- Step 1 Feeding equipment, 112-Step 1 adsorption tower, 113-Step 1 discharge equipment, 114-Step 1 buffer silo, 115-Process 1 discharge equipment, 116-Process 1 net flue gas, 117-Process 1 original Flue gas, 118-process 1 activated carbon storage, 119-process 1 belt scale, 120-process 2 flue gas purification device, 121-process 2 feeding equipment, 122-process 2 adsorption tower, 123-process 2 discharge equipment, 124 -Process 2 buffer silo, 125-process 2 unloading equipment, 126-process 2 net flue gas, 127-process 2 original flue gas, 128-process 2 activated carbon silo, 129-process 2 belt scale, 10-computer subsystem ,1 00-main control unit, 1011-process 1 control unit, 101n-process n control unit, 102-activation subsystem control unit, 103-sintering process control unit, 104-complementary carbon control unit, 4-sintering process flue gas Purification device, 41-sintering process feeding equipment, 42-sintering process adsorption tower, 43-sintering process discharge equipment, 44-sintering process raw flue gas, 45-sintering process net flue gas.
具体实施方式Detailed ways
图2为本申请实施例一提供的多工序烟气净化系统的结构示意图；图3为本申请实施例一提供的多工序烟气净化系统的结构框图。2 is a schematic structural view of a multi-process flue gas purification system according to Embodiment 1 of the present application; FIG. 3 is a structural block diagram of a multi-process flue gas purification system according to Embodiment 1 of the present application.
参见图2，本申请实施例提供的多工序烟气净化系统，包括：活性炭集中解析活化子系统2，活性炭输送子系统3，以及与各工序对应的烟气净化装置，每一烟气净化装置分别通过活性炭输送子系统3与活性炭集中解析活化子系统2连接。Referring to FIG. 2, a multi-process flue gas purification system provided by an embodiment of the present application includes: an activated carbon centralized analytical activation subsystem 2, an activated carbon delivery subsystem 3, and a flue gas purification device corresponding to each process, and each flue gas purification device. The activated carbon delivery subsystem 3 is connected to the activated carbon centralized analytical activation subsystem 2, respectively.
在本实施例中，为了提高钢铁厂内烟气净化的效率，在全厂设置一个活性炭集中解析活化子系统2，每一个工序处设置的烟气净化装置分别与同一个活性炭集中解析活化子系统2连通，即形成一对多的结构关系。In the present embodiment, in order to improve the efficiency of flue gas purification in the steel plant, a activated carbon centralized analytical activation subsystem 2 is disposed in the whole plant, and the flue gas purification devices provided at each process are respectively combined with the same activated carbon centralized analytical activation subsystem. 2 connected, that is, a one-to-many structural relationship is formed.
例如，如图2所示的多工序烟气净化系统，工序1烟气净化装置110、工序 2烟气净化装置120，分别通过活性炭输送子系统3与活性炭集中解析活化子系统2呈现串联结构，每一烟气净化装置排放的污染活性炭被分别输送至活性炭集中解析活化子系统2处，经解析活化后得到的活化活性炭再分别输送至每一工序中的烟气净化装置内，实现活性炭的循环利用。For example, as shown in FIG. 2, the multi-step flue gas purification system, the process 1 flue gas purification device 110, and the process 2 flue gas purification device 120 respectively have a tandem structure through the activated carbon transport subsystem 3 and the activated carbon centralized analytical activation subsystem 2, The polluted activated carbon discharged from each flue gas purification device is separately transported to the activated carbon centralized analytical activation subsystem 2, and the activated activated carbon obtained after the analytical activation is separately transported to the flue gas purification device in each process to realize the circulation of the activated carbon. use.
需要说明的是，图2仅是示例性地示出工序1烟气净化装置110和工序2烟气净化装置120与活性炭集中解析活化子系统2之间的关系。而根据钢铁厂的生产过程，实际上会存在多个产生烟气的工序。因此，多工序烟气净化系统中会包括多个工序对应的烟气净化装置。本实施例中，仅以多工序烟气净化系统包括工序1烟气净化装置110和工序2烟气净化装置120进行举例说明。It should be noted that FIG. 2 is merely an example showing the relationship between the step 1 flue gas purification device 110 and the step 2 flue gas purification device 120 and the activated carbon concentration analysis activation subsystem 2. According to the production process of the steel plant, there are actually many processes for generating flue gas. Therefore, the multi-process flue gas purification system includes a plurality of flue gas purification devices corresponding to the processes. In the present embodiment, only the multi-step flue gas purification system includes the step 1 flue gas purifying device 110 and the step 2 flue gas purifying device 120.
为实现每一个烟气净化装置与活性炭集中解析活化子系统2之间活性炭的循环利用，所采用的方式是利用活性炭输送子系统3进行运输。由于在钢铁厂内，相邻两个烟气净化装置之间的距离较远，而活性炭集中解析活化子系统2与每一个烟气净化装置呈现串联关系，使得不同烟气净化装置与活性炭集中解析活化子系统2之间的距离也不相同。而为了实现活性炭的高效运输和循环利用，通过皮带或运输机运输的方式，可能并不适用于距离较远的情况。因此，本实施例中，活性炭输送子系统3除了选用皮带、输送机外，还可选用汽车来运输，避免在全厂内设置输送机或皮带，增加占地面积，影响全厂内的结构布局，也可提高输送较远距离的活性炭的效率。In order to realize the recycling of activated carbon between each flue gas purification device and the activated carbon centralized analytical activation subsystem 2, the method adopted is to transport by the activated carbon conveying subsystem 3. Because in the steel plant, the distance between two adjacent flue gas purification devices is far, and the activated carbon centralized analytical activation subsystem 2 and each flue gas purification device are in a series relationship, so that different flue gas purification devices and activated carbon are analyzed in a concentrated manner. The distance between the activation subsystems 2 is also different. In order to achieve efficient transportation and recycling of activated carbon, transportation by belt or conveyor may not be suitable for long distances. Therefore, in this embodiment, in addition to the belt and the conveyor, the activated carbon conveying subsystem 3 can also be transported by using a car to avoid setting up a conveyor or a belt in the whole plant, increasing the floor space and affecting the structural layout of the whole plant. It can also increase the efficiency of the activated carbon transporting a long distance.
具体地，活性炭集中解析活化子系统2包括解析塔23，用于对各工序对应的烟气净化装置排放的污染活性炭进行解析活化，以便于得到活化活性炭进行循环利用；设置在解析塔23入口端的给料装置22，用于将各工序对应的烟气净化装置排放的总污染活性炭，按照一定频率或流量送入到解析塔23中，以适应解析塔23的解析活化频率；设置在解析塔23出口端的排料装置24，排料装置24通过活性炭输送子系统3与各工序对应的烟气净化装置的入口端连接，排料装置24用于将解析塔23经过解析活化后得到的活化活性炭以一定的频率或流量排放到活性炭输送子系统3内，进而运输至每个工序中的烟气净化装置；设置在各工序对应的烟气净化装置的出口端与给料装置之间的总活性炭仓25，用于收集各工序中烟气净化装置排放的污染活性炭；以及，设置在总活性炭仓25与给料装置22之间的皮带秤26，用于将总活性炭仓25内收集的所有污染活性炭运送至活性炭输送子系统3中，进而送入到设置在给料装置22上方的缓冲仓21内，给料装置22实现缓冲仓21与解析塔23的连通，以通过给料装置22，按照一定流量或频率将污染活性炭送入到解析塔23内。Specifically, the activated carbon concentration analysis activation subsystem 2 includes an analysis tower 23 for analyzing and activating the polluted activated carbon discharged from the flue gas purification device corresponding to each process, so as to obtain activated activated carbon for recycling; and is disposed at the inlet end of the analytical tower 23. The feeding device 22 is configured to send the total polluted activated carbon discharged from the flue gas purifying device corresponding to each step to the analytical tower 23 at a constant frequency or flow rate to accommodate the analytical activation frequency of the analytical tower 23; The discharge device 24 at the outlet end, the discharge device 24 is connected to the inlet end of the flue gas purification device corresponding to each process through the activated carbon delivery subsystem 3, and the discharge device 24 is used to activate the activated carbon obtained by analytically activating the analytical column 23. A certain frequency or flow rate is discharged into the activated carbon conveying subsystem 3, and then transported to the flue gas purifying device in each process; the total activated carbon storage chamber disposed between the outlet end of the flue gas purifying device corresponding to each process and the feeding device 25, for collecting polluted activated carbon discharged from the flue gas purification device in each process; and, being disposed in the total activated carbon cartridge 25 and the feedstock A belt weigher 26 is disposed between 22 for transporting all contaminated activated carbon collected in the total activated carbon cartridge 25 to the activated carbon conveying subsystem 3, and then to the buffer tank 21 disposed above the feeding device 22, feeding The device 22 effects communication between the buffer chamber 21 and the analytical column 23 to feed the contaminated activated carbon into the analytical column 23 at a constant flow rate or frequency through the feed device 22.
工序1烟气净化装置110包括：工序1给料设备111、工序1吸附塔112、工序1排料设备113、工序1缓冲料仓114、工序1卸料设备115、工序1活性炭仓 118和工序1皮带秤119。在烟气净化装置运行过程中，工序1活性炭仓118用于承装由活性炭集中解析活化子系统2运输来的活化活性炭，经过工序1皮带秤119运送至活性炭输送子系统3，由于烟气净化装置的自身高度较高，因此，为了将低处的活化活性炭输送至位于高处的工序1缓冲仓，此处，活性炭输送子系统3可选用输送机。储存在工序1缓冲仓的活化活性炭经工序1给料设备111进入工序1吸附塔112中，同时，工序1原烟气117也进入工序1吸附塔112中，工序1原烟气117携带的污染物经工序1吸附塔112内的活化活性炭吸附后，得到的工序1净烟气116外排。而吸附有污染物的污染活性炭经过工序1排料设备113排放到工序1缓冲料仓114进行短暂储存，当工序1缓冲料仓114内储存的污染活性炭达到一定量时，由工序1卸料设备115将污染活性炭卸入到活性炭输送子系统3中。此处，为了增加输送量和速率，活性炭输送子系统3可选用汽车，进而利用活性炭输送子系统3将污染活性炭输送至总活性炭仓25内，等待被解析活化处理。The flue gas purification device 110 of the first step includes a step 1 feeding device 111, a step 1 adsorption tower 112, a step 1 discharge device 113, a step 1 buffer silo 114, a step 1 discharge device 115, a process 1 activated carbon cartridge 118, and a process. 1 belt scale 119. In the operation process of the flue gas purification device, the activated carbon storage tank 118 of the process 1 is used to carry the activated activated carbon transported by the activated carbon centralized analytical activation subsystem 2, and is transported to the activated carbon conveying subsystem 3 through the belt scale 119 of the process 1, due to the purification of the flue gas. The height of the device itself is relatively high, therefore, in order to transport the activated activated carbon at a lower position to the buffer tank of the process 1 located at a high place, here, the activated carbon conveying subsystem 3 may be a conveyor. The activated activated carbon stored in the buffer chamber of the first step enters the adsorption tower 112 of the step 1 through the feed device 111 of the first step, and the raw flue gas 117 of the first step also enters the adsorption tower 112 of the first step, and the pollution carried by the raw flue gas 117 of the first step After the object is adsorbed by the activated activated carbon in the adsorption tower 112 in the step 1, the obtained step 1 net flue gas 116 is discharged. The contaminated activated carbon adsorbed with the pollutants is discharged to the buffer silo 114 of the process 1 through the discharge device 113 of the process 1 for short-term storage. When the contaminated activated carbon stored in the buffer silo 114 of the process 1 reaches a certain amount, the unloading device of the process 1 is processed. 115 The contaminated activated carbon is discharged into the activated carbon delivery subsystem 3. Here, in order to increase the conveying amount and rate, the activated carbon conveying subsystem 3 may select an automobile, and then use the activated carbon conveying subsystem 3 to deliver the contaminated activated carbon into the total activated carbon cartridge 25, waiting for the analytical activation treatment.
同样的，工序2烟气净化装置120包括：工序2给料设备121、工序2吸附塔122、工序2排料设备123、工序2缓冲料仓124、工序2卸料设备125、工序2活性炭仓128和工序2皮带秤129工序2。工序2烟气净化装置120对工序2原烟气117进行烟气净化得到工序2净烟气126的过程与工序1烟气净化装置110相同，此处不再赘述。Similarly, the process 2 flue gas purification device 120 includes a process 2 feeding device 121, a process 2 adsorption tower 122, a process 2 discharge device 123, a process 2 buffer silo 124, a process 2 discharge device 125, and a process 2 activated carbon cartridge. 128 and step 2 belt scale 129 step 2. Step 2 The flue gas purification device 120 performs the flue gas purification on the raw flue gas 117 in the step 2, and the process of obtaining the net flue gas 126 in the second step is the same as the flue gas purification device 110 in the first step, and will not be described herein.
如图3所示，为了实现多工序烟气净化系统中各子系统、装置的精准控制，提高运行效率，本实施例提供的多工序烟气净化系统还包括计算机子系统10，计算机子系统10配置有主控制单元100，设置在活性炭集中解析活化子系统的活化子系统控制单元102，用于控制活性炭集中解析活化子系统2中各结构的工作状态及调整工作参数；以及设置在每一工序中烟气净化装置内的工序控制单元，用于控制相应烟气净化装置中各结构的工作状态及调整工作参数；主控制单元100用于与活化子系统控制单元102和工序控制单元进行双向数据传输，通过对数据的计算和分析，控制活化子系统控制单元102和工序控制单元执行相应指令，进而实现对整个多工序烟气净化系统的统一精准控制，提高烟气净化的运行效率。As shown in FIG. 3, in order to realize precise control of each subsystem and device in the multi-process flue gas purification system and improve operation efficiency, the multi-process flue gas purification system provided in this embodiment further includes a computer subsystem 10, and the computer subsystem 10 The main control unit 100 is disposed, and the activation subsystem control unit 102 is disposed in the activated carbon concentration analysis activation subsystem for controlling the working state of each structure in the activated carbon centralized analysis activation subsystem 2 and adjusting the working parameters; and setting in each process The process control unit in the middle flue gas purification device is configured to control the working state of each structure in the corresponding flue gas purifying device and adjust the working parameters; the main control unit 100 is configured to perform bidirectional data with the activation subsystem control unit 102 and the process control unit. Transmission, through the calculation and analysis of the data, the control activation subsystem control unit 102 and the process control unit execute corresponding instructions, thereby achieving uniform and precise control of the entire multi-process flue gas purification system, and improving the operation efficiency of the flue gas purification.
具体地，在实际应用中，每一工序处的工序控制单元具有以下功能，即确定当前工序中烟气净化装置在t ni时刻对应的活性炭循环流量W Xn(tni)；以及，将当前工序中烟气净化装置的活性炭循环流量W Xn(tni)发送至主控制单元100；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，i为发送相应数据的时刻，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间。 Specifically, in practical applications, the process control unit at each process has the following functions, that is, determining the activated carbon circulation flow W Xn(tni) corresponding to the flue gas purification device at the time t ni in the current process; and, in the current process The activated carbon circulation flow rate W Xn(tni) of the flue gas purification device is sent to the main control unit 100; wherein n is the serial number of each process in the multi-process flue gas purification system; t ni =tT ni , i is the time at which the corresponding data is transmitted, T ni is the time during which the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon concentration analysis activation subsystem.
本实施例中，每一工序处的工序控制单元将对应的烟气净化装置内的活性炭 流量发送至主控制单元100，以便主控制单元100根据所有工序中烟气净化装置的活性炭流量进行计算和分析，以调整相应工序中烟气净化装置的工作状态，使得整体的多工序烟气净化系统的运行效率达到最大。In this embodiment, the process control unit at each process sends the activated carbon flow rate in the corresponding flue gas purification device to the main control unit 100, so that the main control unit 100 calculates and calculates the activated carbon flow rate of the flue gas purification device in all processes. The analysis is to adjust the working state of the flue gas purification device in the corresponding process, so that the operating efficiency of the overall multi-process flue gas purification system is maximized.
为此，如图7所示，相应工序n对应的工序控制单元按照如下方法确定当前工序中烟气净化装置在t ni时刻对应的活性炭循环流量W Xn(tni)： Therefore, as shown in FIG. 7, the process control unit corresponding to the corresponding process n determines the activated carbon circulation flow W Xn(tni) corresponding to the flue gas purification device at the time t ni in the current process as follows:
S21、根据工序n在生产过程中产生的原烟气总量V n，以及根据下式，计算t ni时刻对应的原烟气中的SO 2和NO X总流量； S21, according to step n generated in the production process of the original total amount of flue gas V n, according to the following formula and calculate the total SO 2 and NO X flow rate corresponding to the original flue t ni in time;
W Sn(tni)＝V n×C Sn/10 6； W Sn(tni) = V n × C Sn /10 6 ;
W Nn(tni)＝V n×C Nn/10 6； W Nn(tni) = V n × C Nn /10 6 ;
式中，W Sn(tni)为工序n在t ni时刻对应的原烟气中的SO 2总流量，单位kg/h；W Nn(tni)为工序n在t ni时刻对应的原烟气中的NO X总流量，单位kg/h；V n为t ni时刻对应的原烟气总量，单位Nm 3/h；C Sn为工序n在t ni时刻对应的原烟气中的SO 2浓度，单位mg/Nm 3；C Nn为工序n在t ni时刻对应的原烟气中的NO X浓度，单位mg/Nm 3。 Where W Sn(tni) is the total flow rate of SO 2 in the raw flue gas corresponding to the step n at time t ni , in units of kg/h; W Nn(tni) is the original flue gas corresponding to the step n at time t ni the total NO X flow rate, the unit kg / h; V n is the total original flue t ni corresponding to the time, the unit Nm 3 / h; 2 concentration in the raw flue gas of step n C Sn at time t ni corresponding to SO unit mg / Nm 3; NO X concentration in the raw flue gas C Nn to step n at time t ni corresponding to the units mg / Nm 3.
由于钢铁厂产生的污染物的主要成分为粉尘、SO 2和NO X，另外还有少量VOCs、二噁英和重金属等，但因为各工序自带除尘功能，且SO 2和NO X以外的污染物含量较少，所以，烟气净化装置主要去除烟气中的SO 2和NO X，因此，可根据进入到吸附塔的烟气中携带的SO 2和NO X的量来推算理论上所需要的活性炭的量，以达到最佳的吸附效果，既不会出现吸附饱和，也不会出现吸附不足的情况。 Since the main component of steel plant dust is generated pollutants, SO 2 and NO X, in addition to a small amount of VOCs, dioxins and heavy metals, but because each step carrying dust removal function, pollutants other than SO 2 and NO X, and content is less, so that the flue gas purification device that mainly removes the flue gas NO X and sO 2, and therefore, can be estimated theoretically required according to the amount of sO 2 and NO X into the adsorption tower of the flue gas carried in The amount of activated carbon is used to achieve the best adsorption effect, and neither adsorption saturation nor insufficient adsorption occurs.
S22、根据原烟气中的SO 2和NO X总流量，以及下式，计算t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)； S22, according to the total flow X and SO 2 in the flue gas NO original, and the following equation, calculated t ni corresponding to the time step n flue gas purification device activated circulation flow rate W Xn (tni);
W Xn(tni)＝K 1×W Sn(tni)+K 2×W Nn(tni)； W Xn(tni) = K 1 × W Sn(tni) + K 2 × W Nn(tni) ;
式中，W Xn(tni)为工序n中烟气净化装置对应的t ni时刻的活性炭循环流量，单位kg/h；K 1为第一系数，取值范围为15～21；K 2为第二系数，取值范围为3～5。 In the formula, W Xn(tni) is the circulating flow rate of activated carbon at t ni time corresponding to the flue gas purification device in process n, unit kg/h; K 1 is the first coefficient, and the value ranges from 15 to 21; K 2 is the first The two coefficients are in the range of 3 to 5.
由于活性炭在吸附塔内为流动状态，烟气也为流动状态，为了使得吸附塔内的活性炭能够对进入吸附塔的烟气进行最佳的吸附作用，因此，需要活性炭的流动状态与烟气的流动状态满足一定的比例关系，即烟气净化装置中活性炭循环流量与原烟气中的SO 2和NO X总流量存在一定的比例关系。 Since the activated carbon is in a flowing state in the adsorption tower and the flue gas is also in a flowing state, in order to enable the activated carbon in the adsorption tower to optimally adsorb the flue gas entering the adsorption tower, the flow state of the activated carbon and the flue gas are required. flow state satisfies a certain proportional relationship, i.e., flue gas cleaning certain ratio between SO 2 and NO X flow rate total flow circulation apparatus charcoal original flue gas.
每一工序处的工序控制单元分别将当前工序中烟气净化装置的活性炭循环流量W Xn(tni)发送至主控制单元100，例如，工序1控制单元1011将工序1烟气净化装置110的活性炭循环流量W X1(t1i)发送至主控制单元100；工序2控制单元1012将工序2烟气净化装置120的活性炭循环流量W X2(t2i)发送至主控制单元100；工 序n控制单元101n将工序n烟气净化装置的活性炭循环流量W Xn(tni)发送至主控制单元100。 The process control unit at each process sends the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the current process to the main control unit 100, for example, the process 1 control unit 1011 converts the activated carbon of the process 1 flue gas purification device 110. The circulation flow rate W X1 (t1i) is sent to the main control unit 100; the process 2 control unit 1012 transmits the activated carbon circulation flow rate W X2 (t2i) of the process 2 flue gas purification device 120 to the main control unit 100; the process n control unit 101n processes the process The activated carbon circulation flow rate W Xn(tni) of the n flue gas purification device is sent to the main control unit 100.
主控制单元100获取到t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)，根据所有工序中烟气净化装置的活性炭循环流量W Xn(tni)，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0。该循环量W X0为活性炭集中解析活化子系统的理论活性炭循环量，根据理论值可准确地控制活性炭集中解析活化子系统的运行状态和工作参数。 The main control unit 100 acquires the activated carbon to the circulating flow rate W Xn (tni) t ni corresponding to the time step n, flue gas cleaning equipment, activated carbon in accordance with all the processes in the circulation flow rate W Xn (tni) flue gas purification device, determining a current time t The corresponding activated carbon concentrates on the activated carbon circulation flow W X0 of the activation subsystem. The circulation amount W X0 is the theoretical activated carbon circulation amount of the activated carbon centralized analytical activation subsystem, and the operating state and working parameters of the activated carbon centralized analytical activation subsystem can be accurately controlled according to the theoretical value.
具体地，主控制单元100按照下式，根据工序n中烟气净化装置的活性炭循环流量W Xn(tni)，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； Specifically, the main control unit 100 determines, according to the following formula, the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t according to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n;
W X0＝∑W Xn(tni)＝∑W Xn(t-Tni)； W X0 = ∑W Xn(tni)= ∑W Xn(t-Tni) ;
式中，t为当前时刻，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间，由活性炭输送子系统3提供。 Where t is the current time, and T ni is the time during which the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon concentration analysis activation subsystem at time i, and is provided by the activated carbon delivery subsystem 3.
活性炭集中解析活化子系统的活性炭循环流量W X0为各工序中烟气净化装置的活性炭循环流量的总和，但是在计算活性炭集中解析活化子系统2的理论活性炭循环流量时的当前时刻t，并非是各工序控制单元确定相应各工序中烟气净化装置的活性炭循环量以及发送数据的时刻t ni。这是由于烟气净化装置排出的污染活性炭运输至活性炭集中解析活化子系统2需要耗费一定的时间，且在不同时刻，由不同工序运输至活性炭集中解析活化子系统2所需的时间也不相同。而每一工序在生产过程中产生的烟气量和污染物浓度是时刻变化的，会导致在不同时刻烟气净化装置内的活性炭循环流量发生变化，进而无法保证在当前时刻t，活性炭集中解析活化子系统2中接收的污染活性炭恰好为相应工序中烟气净化装置排放的污染活性炭，即无法保证活性炭集中解析活化子系统2接收的污染活性炭的循环流量为该活性炭实际在相应烟气净化装置时的活性炭循环流量，而当前时刻t活化子系统控制单元102获取的活性炭循环流量，需要相应工序在经过运输时间T ni之后才能获取到，即对多工序烟气净化系统的精准控制需要在延后T ni时段之后，这样会降低运行效率，导致得到的活性炭集中解析活化子系统的理论活性炭循环流量W X0不准确。 The activated carbon circulation flow W X0 of the activated carbon centralized analysis activation subsystem is the sum of the activated carbon circulation flow rate of the flue gas purification device in each process, but the current time t when calculating the theoretical activated carbon circulation flow of the activation activated subsystem 2 in the activated carbon concentration is not Each of the process control units determines the amount of activated carbon circulation of the flue gas purification device in each of the respective processes and the time t ni at which the data is transmitted. This is because it takes a certain time for the polluted activated carbon discharged from the flue gas purification device to be transported to the activated carbon concentration analysis activation subsystem 2, and the time required for the different processes to be transported to the activated carbon centralized analytical activation subsystem 2 at different times is also different. . The amount of flue gas and the concentration of pollutants generated during the production process vary from time to time, which may cause changes in the circulating flow of activated carbon in the flue gas purification device at different times, and thus cannot guarantee the centralized analysis of activated carbon at the current time t. The polluted activated carbon received in the activation subsystem 2 is just the polluted activated carbon discharged from the flue gas purification device in the corresponding process, that is, the circulating flow rate of the contaminated activated carbon received by the activated carbon concentration analysis activation subsystem 2 cannot be ensured as the activated carbon actually in the corresponding flue gas purification device. When the activated carbon circulation flow rate, and the current time t activates the activated carbon circulation flow obtained by the subsystem control unit 102, the corresponding process needs to be obtained after the transportation time T ni , that is, the precise control of the multi-process flue gas purification system needs to be extended. After the T ni period, this will reduce the operating efficiency, resulting in an inaccurate theoretical activated carbon circulation flow W X0 of the activated activated carbon concentration analysis activation subsystem.
例如，计算活性炭集中解析活化子系统2的理论活性炭循环流量时的当前时刻t为10:00，工序1中烟气净化装置排放的污染活性炭运输至活性炭集中解析活化子系统的时间T 1i为0.5小时，那么，工序1控制单元1011需将t 1i为9:30时刻对应的工序1中烟气净化装置的活性炭循环流量W X1(t1i)发送至主控制单元100；再例如，计算活性炭集中解析活化子系统2的理论活性炭循环流量时的当前时刻 t为14:20，工序2中烟气净化装置排放的污染活性炭运输至活性炭集中解析活化子系统的时间T 2i为40分钟，那么，工序2控制单元1012需将t 2i为13:40时刻对应的工序2中烟气净化装置的活性炭循环流量W X2(t2i)发送至主控制单元100。 For example, the current time t when calculating the circulating flow rate of the activated carbon of the activated carbon concentration analysis activation subsystem 2 is 10:00, and the time T 1i of the polluted activated carbon discharged from the flue gas purification device in the process 1 to the activated carbon concentration analysis activation subsystem is 0.5. h, then the step 1011 the control unit 1 need to be 9.30 t 1i corresponding to the time step 1 charcoal circulation flow rate W X1 (t1i) flue gas cleaning apparatus 100 transmits to the main control unit; For another example, active carbon concentration calculating analytical The current time t of the theoretical activated carbon circulation flow of the activation subsystem 2 is 14:20, and the time T 2i of the contaminated activated carbon discharged from the flue gas purification device in the process 2 to the activated carbon centralized analytical activation subsystem is 40 minutes, then, the process 2 The control unit 1012 transmits the activated carbon circulation flow rate W X2 (t2i) of the flue gas purification device in the step 2 corresponding to the time T 2i at 13:40 to the main control unit 100.
因此，为了确保多工序烟气净化系统的运行效率，以及活化子系统控制单元102获取的数据，即各工序中烟气净化装置的活性炭循环流量W Xn(tni)的准确性，以便获取的数据能够准确地表示当前时刻t活性炭集中解析活化子系统的活性炭循环流量W X0，因此，需要获取在当前时刻t提前运输时间T ni这一时间段对应时刻的各工序中烟气净化装置的活性炭循环流量，即利用W Xn(t-Tni)折算成当前时刻t对应的各工序中烟气净化装置的活性炭循环流量。 Therefore, in order to ensure the operating efficiency of the multi-process flue gas purification system, and the data acquired by the activation subsystem control unit 102, that is , the accuracy of the activated carbon circulation flow W Xn(tni) of the flue gas purification device in each process, in order to obtain the data. It can accurately represent the activated carbon circulating flow W X0 of the activation subsystem of the activated carbon concentration at the current time t. Therefore, it is necessary to acquire the activated carbon circulation of the flue gas purification device in each process corresponding to the time period of the transportation time T ni at the current time t. The flow rate, that is, the flow rate of the activated carbon circulation of the flue gas purification device in each step corresponding to the current time t is converted by W Xn(t-Tni) .
当主控制单元100确定出活性炭集中解析活化子系统的活性炭循环流量W X0之后，需要根据该数据调整皮带秤26的下料流量，以根据皮带秤26的下料流量调整解析塔23的给料装置22和排料装置24的下料流量，使得皮带秤26的下料流量、给料装置22的下料流量和排料装置24的下料流量，与活性炭集中解析活化子系统2的理论活性炭循环流量相等，达到精准控制多工序烟气净化系统的效果。 After the main control unit 100 determines that the activated carbon concentrates on the activated carbon circulating flow W X0 of the activation subsystem, it is necessary to adjust the blanking flow rate of the belt scale 26 according to the data to adjust the feeding device of the analytical tower 23 according to the blanking flow rate of the belt scale 26 . 22 and the discharge flow rate of the discharge device 24, such that the discharge flow rate of the belt balance 26, the discharge flow rate of the feeding device 22, and the discharge flow rate of the discharge device 24, and the theoretical activated carbon cycle of the activated carbon concentration analysis activation subsystem 2 The flow rate is equal, achieving the effect of accurately controlling the multi-process flue gas purification system.
在实际运行时，皮带秤26的实际运行频率可能无法达到准确控制的程度，因此，为了各工序的烟气净化装置的活性炭循环流量能够与活性炭集中解析活化子系统2的活性炭循环流量相同，使得整个多工序烟气净化系统能够实现同步运行，避免出现因活性炭集中解析活化子系统2运输的活化活性炭的量，不足以支撑各工序中烟气净化装置处吸附烟气的量，降低吸附效果，或者出现活性炭集中解析活化子系统2运输的活化活性炭的量过多，导致各工序中烟气净化装置均处于饱和状态，活化活性炭溢出的情况发生。因此，需要控制皮带秤26的下料流量W C与活性炭集中解析活化子系统的活性炭循环流量W X0相等。 In actual operation, the actual operating frequency of the belt scale 26 may not be able to achieve an accurate degree of control. Therefore, the activated carbon circulation flow rate of the flue gas purification device for each process can be the same as the activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem 2, The whole multi-process flue gas purification system can realize synchronous operation, avoiding the amount of activated activated carbon transported by the activated carbon centralized analytical activation subsystem 2, which is insufficient to support the amount of adsorbed flue gas at the flue gas purification device in each process, and reduce the adsorption effect. Or the amount of activated activated carbon transported by the activated carbon concentration analysis activation subsystem 2 is too large, so that the flue gas purification devices in each process are in a saturated state, and the activated activated carbon overflows. Therefore, it is necessary to control the blanking flow rate W C of the belt weigher 26 to be equal to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem.
具体地，活化子系统控制单元102根据活性炭集中解析活化子系统的活性炭循环流量W X0调整皮带秤26的下料流量W C，使得皮带秤26的下料流量逐渐与活性炭集中解析活化子系统2的活性炭循环流量相等，确定W C＝W X0时对应的皮带秤26的运行频率f c。该运行频率f c为皮带秤26的理论运行频率，也即能够使得多工序烟气净化系统实现同步运行的运行频率。 Specifically, the activation subsystem control unit 102 adjusts the blanking flow rate W C of the belt scale 26 according to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem, so that the blanking flow rate of the belt scale 26 is gradually combined with the activated carbon concentration analysis activation subsystem 2 The activated carbon circulation flow is equal, and the operating frequency f c of the corresponding belt scale 26 when W C = W X0 is determined. The operating frequency f c is the operating frequency of the theoretical belt scale 26, i.e., step enables multiple operating frequency flue gas purification system to achieve synchronous operation.
主控制单元100随即获取皮带秤26的运行频率f c，根据皮带秤26的运行频率f c，向活化子系统控制单元102发送调整指令，以使活化子系统控制单元102调整给料装置22的给定频率f g和排料装置24的给定频率f p，以实现对多工序烟气净化系统的控制。 The main control unit 100 then acquires the belt weigher 26 running frequency f c, the frequency f c of the operating belt scale 26, the sub control unit 102 transmits the activation instruction to adjust to the activated sub-system control unit 102 to adjust the feed apparatus 22 given frequency f g and discharge device 24 of a given frequency f p, in order to achieve control of multiple process flue gas purification system.
具体地，本实施例中，主控制单元100根据获取到的数据，对数据进行分析 和计算，根据结果生成控制指令，以控制活化子系统控制单元102执行相应操作。因此，为准确地根据皮带秤26的运行频率f c，调整给料装置22的给定频率f g和排料装置24的给定频率f p，主控制单元100被配置为执行以下程序步骤： Specifically, in this embodiment, the main control unit 100 analyzes and calculates data according to the acquired data, and generates a control instruction according to the result to control the activation subsystem control unit 102 to perform corresponding operations. Therefore, exactly according to the operation frequency f c belt scale 26, adjusting the feed means to a predetermined frequency 22 f g and discharge device 24 for a given frequency f p, the main control unit 100 is configured to execute the following program steps:
S61、确定皮带秤的下料流量W C＝K c×f c，给料装置的下料流量W G＝K g×f g，排料装置的下料流量W P＝K p×f p；式中，Kc、K g和K p均为常数，与皮带秤26的宽度、给料装置22的出口宽度、排料装置24的出口宽度、电机及变频器参数、活性炭比重等有关。 S61, determining a blanking flow rate of the belt scale W C = K c × f c , a discharge flow rate of the feeding device W G = K g × f g , a discharge flow rate of the discharging device W P = K p × f p ; In the formula, Kc, K g and K p are constant, and are related to the width of the belt scale 26, the outlet width of the feeding device 22, the outlet width of the discharge device 24, the motor and the frequency converter parameters, and the specific gravity of the activated carbon.
由于皮带秤26、给料装置22、排料装置24均为由电机带动物料运输的供料设备，电机由变频器拖动，变频器的运行频率决定其转速，使得皮带秤26、给料装置22、排料装置24的物料输送流量与电机转速成正比，即下料流量与电机的转速成正比。Since the belt scale 26, the feeding device 22, and the discharging device 24 are all feeding devices transported by the motor with animal materials, the motor is dragged by the frequency converter, and the running frequency of the frequency converter determines the rotation speed thereof, so that the belt scale 26 and the feeding device 22. The material delivery flow rate of the discharge device 24 is proportional to the motor rotation speed, that is, the discharge flow rate is proportional to the rotation speed of the motor.
S62、控制活性炭集中解析活化子系统的给料装置、排料装置和皮带秤的下料流量相同，使得W G＝W P＝W C＝W X0。 S62. Controlling the activated carbon centralized analysis of the activation subsystem, the feeding device, the discharging device and the belt weighing flow are the same, such that W G = W P = W C = W X0 .
根据上述介绍，为了各工序的烟气净化装置的活性炭循环流量能够与活性炭集中解析活化子系统2的活性炭循环流量相同，使得整个多工序烟气净化系统能够实现同步运行，需要根据该活性炭集中解析活化子系统2的理论活性炭循环流量W X0调整皮带秤26的下料流量，再根据皮带秤26的下料流量调整解析塔23的给料装置22和排料装置24的下料流量，使得皮带秤26的下料流量W C、给料装置22的下料流量W G和排料装置24的下料流量W P，与活性炭集中解析活化子系统的理论活性炭循环流量W X0相等。 According to the above introduction, the circulation flow rate of the activated carbon for the flue gas purification device of each process can be the same as the circulation flow rate of the activated carbon of the activated carbon concentration analysis activation subsystem 2, so that the entire multi-process flue gas purification system can realize synchronous operation, and needs to be analyzed according to the activated carbon concentration. The theoretical activated carbon circulation flow rate W X0 of the activation subsystem 2 adjusts the discharge flow rate of the belt scale 26, and then adjusts the discharge flow rate of the feeding device 22 and the discharge device 24 of the analytical tower 23 according to the discharge flow rate of the belt balance 26, so that the belt The discharge flow rate W C of the scale 26, the discharge flow rate W G of the feed device 22, and the discharge flow rate W P of the discharge device 24 are equal to the theoretical activated carbon circulation flow rate W X0 of the activated carbon concentration analysis activation subsystem.
S63、根据上式，得到给料装置的给定频率f g与皮带秤的运行频率f c之间满足下式关系：
Figure PCTCN2018083579-appb-000003
以使根据上式及皮带秤的运行频率f c，调整给料装置的给定频率f g；以及， S63,, according to the above formula, to obtain a given frequency feed device satisfies the following relationship of f g between the belt scale operating frequency f c:
Figure PCTCN2018083579-appb-000003
In order to adjust the given frequency f g of the feeding device according to the above formula and the operating frequency f c of the belt weigher;
得到排料装置的给定频率f p与皮带秤的运行频率f c之间满足下式关系：
Figure PCTCN2018083579-appb-000004
以使根据上式及皮带秤的运行频率f c，调整排料装置的给定频率f p。 The relationship between the given frequency f p of the discharge device and the operating frequency f c of the belt scale is obtained:
Figure PCTCN2018083579-appb-000004
In order to adjust the given frequency f p of the discharge device according to the above formula and the operating frequency f c of the belt weigher.
根据给料装置22的给定频率f g、排料装置24的给定频率f p与皮带秤26的运行频率f c之间的比例关系，即可将f g、f p调整至与f c相等，进而可保证在实际运行中，皮带秤26的下料流量W C、给料装置22的下料流量W G和排料装置24的下料流量W P，与活性炭集中解析活化子系统的理论活性炭循环流量W X0相等，使得活性炭集中解析活化子系统的理论活性炭循环流量W X0与各工序的烟气净化装置的活性炭循环流量达到平衡，从而保证整个多工序烟气净化系统能够实现 同步运行，运行效率最佳。 According to the given frequency f g of the feeding device 22, the proportional relationship between the given frequency f p of the discharging device 24 and the operating frequency f c of the belt scale 26, f g , f p can be adjusted to f c Equally, in turn, in the actual operation, the blanking flow rate W C of the belt scale 26, the blanking flow rate W G of the feeding device 22, and the blanking flow rate W P of the discharging device 24, and the activated carbon centralized analytical activation subsystem activated carbon is equal to the theoretical W X0 circulation flow, such that the theoretical activated charcoal concentrate circulation rate W X0 parsing subsystem activated charcoal and the circulation flow rate of the flue gas purification device in each step to reach equilibrium, so as to ensure the entire multi-step gas purification system to achieve synchronous operation , the operating efficiency is best.
由于污染活性炭经过解析塔23解析活化处理后，重量会发生变化，在排放活化活性炭时也会造成活性炭的些许浪费，因此，为了保持解析塔23的给料装置22的下料流量与排料装置24的下料流量的平衡，需要为活性炭集中解析活化子系统2补充新活性炭。Since the contaminated activated carbon is subjected to analysis and activation treatment by the analytical tower 23, the weight changes, and a slight waste of the activated carbon is also caused when the activated activated carbon is discharged. Therefore, in order to maintain the discharge flow rate and the discharge device of the feeding device 22 of the analytical tower 23 The balance of the discharge flow rate of 24 requires the addition of new activated carbon to the activated carbon concentration analysis activation subsystem 2.
本实施例中，补充新活性炭的补充点位于活性炭集中解析活化子系统2，即本实施例提供的活性炭集中解析活化子系统2还包括：设置在总活性炭仓25上方的新活性炭补充装置29。In this embodiment, the supplemental point of the new activated carbon is located in the activated carbon concentration analysis activation subsystem 2, that is, the activated carbon concentration analysis activation subsystem 2 provided in the embodiment further includes: a new activated carbon replenishing device 29 disposed above the total activated carbon cartridge 25.
本实施例将补充新活性炭的装置设置在总活性炭仓25处，这是由于总活性炭仓25用于接收全厂各工序中烟气净化装置排放的污染活性炭，接收所有的污染活性炭之后被统一运送至解析塔23进行解析活化，得到的活化活性炭再被统一运送至各工序的烟气净化装置内，实现活性炭的循环利用。总活性炭仓25接收所有的污染活性炭，可准确地确定各工序中烟气净化装置的活性炭在吸附烟气以及运输过程中时，总共会损耗多少活性炭，进而可以在总活性炭仓25处统一进行补充，避免因在各工序中烟气净化装置处单独补充活性炭，不仅无法保证每次补充新活性炭的量，也会影响系统整体的运行效率。In this embodiment, the device supplementing the new activated carbon is disposed at the total activated carbon storage tank 25, because the total activated carbon cartridge 25 is used for receiving the polluted activated carbon discharged from the flue gas purification device in all processes of the whole plant, and is uniformly transported after receiving all the contaminated activated carbon. The analytical activated carbon is analyzed and activated, and the activated activated carbon obtained is uniformly transported to the flue gas purification device of each step to realize the recycling of the activated carbon. The total activated carbon cartridge 25 receives all the polluted activated carbon, and can accurately determine how much activated carbon is lost in the adsorption of flue gas and the transportation process of the activated carbon in the flue gas purification device in each process, and can be uniformly supplemented in the total activated carbon storage tank 25 To avoid the addition of activated carbon to the flue gas purification device in each process, it is not guaranteed that the amount of new activated carbon will be replenished each time, and the overall operating efficiency of the system will also be affected.
新活性炭补充装置29内设有补新炭控制单元104，该补新炭控制单元104与主控制单元100进行双向数据传输，补新炭控制单元104用于根据主控制单元100的指令，控制新活性炭补充装置29按照一定的频率为总活性炭仓25补充新活性炭。The new activated carbon replenishing device 29 is provided with a replenishing carbon control unit 104, which performs bidirectional data transmission with the main control unit 100, and the refueling control unit 104 is configured to control the new according to the instruction of the main control unit 100. The activated carbon replenishing device 29 replenishes the new activated carbon cartridge 25 with new activated carbon at a certain frequency.
如果总活性炭仓25处有新活性炭进入后，会改变活性炭集中解析活化子系统的活性炭循环量W X0，因此，在计算W X0时不仅要考虑各工序中烟气净化装置的活性炭循环流量，还要考虑新活性炭补充进总活性炭仓25时的活性炭流量。 If new activated carbon enters the total activated carbon storage tank 25, it will change the activated carbon circulation amount W X0 of the activated carbon concentration analysis activation subsystem. Therefore, when calculating W X0 , it is necessary to consider not only the activated carbon circulation flow rate of the flue gas purification device in each process, but also Consider the flow of activated carbon when the new activated carbon is added to the total activated carbon storage tank 25.
具体地，本实施例中，多工序烟气净化系统的主控制单元100按照以下步骤确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0： Specifically, in this embodiment, the main control unit 100 of the multi-process flue gas purification system determines the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t according to the following steps:
S41、确定新活性炭补充装置的补充新活性炭的补充流量W 补，以根据所述补充流量W 补，控制所述新活性炭补充装置向总活性炭仓内补充新活性炭。 S41, determined to add new makeup flow W complement activated carbon GAC replenishing apparatus, according to complement the supplemental flow W, to control the supply apparatus GAC GAC total activated carbon into the cartridge.
本实施例中，由补新炭控制单元104确定新活性炭补充装置29的补充新活性炭的补充流量W 补。由于活性炭集中解析活化子系统2对所有污染活性炭进行统一解析活化，并将得到的活化活性炭统一运送至各工序，并且，各工序中烟气净化装置处不设置筛选损耗炭，而是在活性炭集中解析活化子系统2进行统一的筛选损耗炭，以保证筛选损耗炭的数据准确性，并且可以提高整体系统的运行效 率。 In this embodiment, a fill control unit 104 determines a new carbon GAC supplementary replenishing device 29 is activated a new makeup flow W complement. Since the activated carbon centralized analytical activation subsystem 2 uniformly analyzes and activates all the polluted activated carbon, and the activated activated carbon is uniformly transported to each process, and the flue gas purification device is not provided with the screening loss carbon in each process, but is concentrated in the activated carbon. The activation subsystem 2 is analyzed to perform uniform screening of charcoal to ensure the accuracy of the data of the screened charcoal and improve the operating efficiency of the overall system.
本实施例中，活性炭集中解析活化子系统2还包括：位于排料装置24下方的筛分装置27和位于筛分装置27下方的活化活性炭仓28，筛分装置27用于对经过解析塔23解析活化后的活性炭进行筛分，得到目标粒度的活化活性炭储存至活化活性炭仓28中，活化活性炭仓28中的活化活性炭即为各工序中烟气净化装置所需活性炭的来源。本实施例中，筛分装置27可为振动筛，也可为其他具有筛分作用的装置，本实施例中不做具体限定。In the present embodiment, the activated carbon concentration analysis activation subsystem 2 further includes: a screening device 27 located below the discharge device 24 and an activated activated carbon cartridge 28 located below the screening device 27, the screening device 27 being used for the parsing tower 23 The activated activated carbon is analyzed for sieving, and the activated activated carbon having the target particle size is obtained and stored in the activated activated carbon storage tank 28. The activated activated carbon in the activated carbon storage tank 28 is the source of the activated carbon required for the flue gas purification device in each process. In this embodiment, the sieving device 27 may be a vibrating screen or other sieving device, which is not specifically limited in this embodiment.
在实际运行中，筛分装置27在对解析后的活性炭进行筛分时，会产生少量的损耗，而该损耗可包括各工序中烟气净化装置在吸附烟气时造成的活性炭损耗、在运输中产生的损耗、在解析塔23中产生的损耗以及经过筛分装置27后产生的损耗。可见，通过设置在活性炭集中解析活化子系统2处的筛分装置27产生的损耗炭量，即为多工序烟气净化系统在运行过程中产生的所有消耗炭量的总和。根据此处产生的消耗炭量，即可准确并快速地确定总活性炭仓25处需要补充的新活性炭量，以保证活性炭集中解析活化子系统的理论活性炭循环流量W X0与各工序的烟气净化装置的活性炭循环流量达到平衡，从而保证整个多工序烟气净化系统能够实现同步运行，运行效率最佳。 In actual operation, the screening device 27 generates a small amount of loss when sieving the analyzed activated carbon, and the loss may include the loss of activated carbon caused by the flue gas purification device in the process of adsorbing the flue gas in the process. The loss generated in the strain, the loss generated in the analytical column 23, and the loss generated after passing through the screening device 27. It can be seen that the amount of carbon loss generated by the screening device 27 disposed at the activation subsystem 2 in the activated carbon concentration is the sum of all the consumed carbon amounts generated during the operation of the multi-process flue gas purification system. According to the amount of carbon consumed here, the amount of new activated carbon needed to be replenished in the total activated carbon storage tank 25 can be accurately and quickly determined to ensure the theoretical activated carbon circulation flow W X0 of the activated carbon concentration analysis activation subsystem and the flue gas purification of each process. The circulating flow rate of the activated carbon of the device is balanced, thereby ensuring that the entire multi-process flue gas purification system can realize synchronous operation and the operation efficiency is optimal.
为此，为了准确地确定单位时间内的新活性炭补充装置29的补充新活性炭的补充流量W 补。如图8所示，本实施例中的活化子系统控制单元102采用如下方法步骤： For this reason, in order to determine a new active carbon in the unit time flow rate of the new supplementary supply apparatus 29 is activated complement W accurately. As shown in FIG. 8, the activation subsystem control unit 102 in this embodiment adopts the following method steps:
S411、根据活性炭集中解析活化子系统的活性炭循环流量W X0，按照下式，确定活性炭集中解析活化子系统中解析塔的活性炭装填料量Q 0； S411, according to the activated carbon circulating flow W X0 of the activated carbon centralized analysis activation subsystem, according to the following formula, determining the activated carbon loading amount Q 0 of the analytical tower in the activated carbon centralized analytical activation subsystem;
Q 0＝W X0×T 0； Q 0 = W X0 × T 0 ;
式中，Q 0为活性炭集中解析活化子系统中解析塔的活性炭装填料量，单位kg；T 0为解析塔内活性炭的停留时间，取值范围4～8，单位h； Wherein, Q 0 is the activated carbon loading amount of the analytical tower in the activated carbon concentration analysis activation subsystem, unit kg; T 0 is the residence time of the activated carbon in the analytical tower, the value ranges from 4 to 8, unit h;
本实施例中，采用进入解析塔中的所有污染活性炭的量与排放的活化活性炭的量之差，确定损耗活性炭量。In this embodiment, the amount of depleted activated carbon is determined by using the difference between the amount of all contaminated activated carbon entering the analytical column and the amount of activated activated carbon discharged.
因此，需要根据活性炭集中解析活化子系统的活性炭循环流量W X0和污染活性炭在解析塔内的停留时间T 0，确定当前时刻t解析塔的活性炭装填料量Q 0。 Therefore, it is necessary to determine the activated carbon loading amount Q 0 of the analytical tower at the current time t according to the activated carbon circulating flow W X0 of the activated carbon concentration analysis and the residence time T 0 of the contaminated activated carbon in the analytical tower.
S412、检测活性炭集中解析活化子系统中活化活性炭仓的实际活性炭料量Q 实； S412, focus detection parse activated charcoal actual quantity of activated carbon in the activated carbon cartridge subsystem real Q;
S413、根据解析塔的活性炭装填料量Q 0和实际活性炭料量Q 实，按照式Q 损＝Q 0-Q 实，确定活性炭经所述筛分装置筛分处理后的损耗活性炭料量Q 损； S413, according to the quantity of activated carbon packed analytical column Q 0 of the activated carbon and the actual real quantity Q, in accordance with the formula Q = Q 0 -Q real loss, determine the loss quantity Q activated charcoal loss after sieving through the sieve processing means ;
由活化子系统控制单元102检测当前时刻t对应的活化活性炭仓的实际活性炭料量Q 实，再根据解析塔23内活性炭装填料量Q 0，即可确定多工序烟气净化系统在一次循环运行时，产生的所有损耗活性炭料量。 Subsystem is activated by the control unit 102 detects the actual current time t activated activated carbon cartridge quantity Q corresponding to the solid, and then run in a multi-step cycle flue gas purification system loaded activated carbon 23 within the desorber quantity Q 0, can be determined according to At the time, all the lost activated carbon was produced.
S414、控制新活性炭补充装置的补充活性炭料量Q 补与损耗活性炭料量Q 损相等，根据调整后的补充活性炭料量Q 补，确定单位时间的新活性炭补充装置的补充新活性炭的补充流量W 补。 S414, new control quantity added activated charcoal with supplementary means loss of activated complement Q loss quantity Q is equal to, activated carbon supplementary quantity Q adjusted up, determining new activated charcoal add new supplementary device makeup flow per unit time W Make up .
经筛分装置27后产生的损耗活性炭料量Q 损，即为新活性炭补充装置29所要实际补充的新活性炭料量。因此，将损耗活性炭料量Q 损作为基准，由补新炭控制单元104控制新活性炭补充装置29按照损耗活性炭料量Q 损确定补充活性炭料量Q 补。当补充料量确定后，即可确定单位时间的补充新活性炭的补充流量W补。 The amount of depleted activated carbon produced by the screening device 27 is Q loss , which is the amount of new activated carbon to be actually replenished by the new activated carbon replenishing device 29. Thus, the loss of activated carbon loss quantity Q as a reference, the new device consists of activated complement new supplementary control unit 104 controls the carbon 29 according to the loss quantity Q activated charcoal added loss quantity Q is determined complement. When the amount of supplementary material is determined, the supplementary flow W supplement of the new activated carbon per unit time can be determined.
当新活性炭补充装置29的补充新活性炭的补充流量W 补确定后，由补新炭控制单元104控制新活性炭补充装置，按照补充流量W 补向总活性炭仓内补充新活性炭。 When the supplemental device is determined to add new activated carbon activated carbon 29 new makeup flow W fill, fill the new activated carbon new supplementary control unit 104 to control means, activated charcoal into the newly added active carbon cartridge according to the total flow rate W added up.
S42、根据工序n中烟气净化装置的活性炭循环流量W Xn(tni)，补充流量W 补，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； S42, according to the activated carbon circulating flow W Xn (tni) of the flue gas purification device in the process n, the supplementary flow W supplement , and the following formula, determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
W X0＝∑W Xn(t-Tni)+W 补。 W X0 = ∑W Xn(t-Tni)+ W complement .
由于总活性炭仓内25包括各工序中烟气净化装置排放的污染活性炭和新补充的新活性炭，在确定活性炭集中解析活化子系统2的理论活性炭循环流量时，要综合考虑上述活性炭循环流量。活性炭集中解析活化子系统2在当前循环时产生损耗炭，随即进行补充，以保证活性炭集中解析活化子系统在下一次循环时对应的活性炭循环流量，与各工序中烟气净化装置中的活性炭循环流量总和相等。由此可见，本实施例通过统一筛选损耗炭，并统一进行补充新活性炭，可保证损耗和补充量的准确性，并可最大程度地减少该操作的时间，进而提高多工序烟气净化系统的运行效率。Since the total activated carbon storage tank 25 includes the polluted activated carbon discharged from the flue gas purification device in each process and the newly added new activated carbon, the above-mentioned activated carbon circulation flow rate should be comprehensively considered when determining the theoretical activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem 2. Activated carbon concentrated analytical activation subsystem 2 generates carbon loss at the current cycle, and then supplements to ensure that the activated carbon concentrates on the activated carbon circulation flow corresponding to the activation subsystem in the next cycle, and the activated carbon circulation flow in the flue gas purification device in each process The sum is equal. It can be seen that the present embodiment can improve the accuracy of the loss and the replenishing quantity by uniformly screening the carbon loss and uniformly supplementing the new activated carbon, and can minimize the time of the operation, thereby improving the multi-process flue gas purification system. operating efficiency.
由以上技术方案可知，本申请实施例提供的多工序烟气净化系统，包括活性炭集中解析活化子系统2，活性炭输送子系统3，以及与各工序对应的烟气净化装置，每一烟气净化装置分别通过活性炭输送子系统3与活性炭集中解析活化子系统2连接，各工序对应的烟气净化装置排放的污染活性炭分别运送至活性炭集中解析活化子系统2的总活性炭仓25，再由解析塔23进行解析活化，得到的活化活性炭再被运送至各工序的烟气净化装置，实现活性炭的循环利用。各工序中 烟气净化装置内设置的工序控制单元将对应烟气净化装置的活性炭循环流量发送至主控制单元100，主控制单元100利用所有工序对应的活性炭循环流量的总和代表活性炭集中解析活化子系统2的活性炭循环流量，并控制设置在活性炭集中解析活化子系统2的活化子系统控制单元102，以调整活性炭集中解析活化子系统2中皮带秤26、给料装置22和排料装置24的给定频率，使得活性炭集中解析活化子系统2处的活性炭循环流量与各工序中烟气净化装置的活性炭循环流量总和实质相等，使得多工序烟气净化系统的吸附部分与解析部分达到同步运行的目的，进而使得活性炭集中解析活化子系统的理论活性炭循环流量W X0与各工序的烟气净化装置的活性炭循环流量达到平衡，提高运行效率。 It can be seen from the above technical solutions that the multi-process flue gas purification system provided by the embodiment of the present application includes the activated carbon centralized analytical activation subsystem 2, the activated carbon conveying subsystem 3, and the flue gas purification device corresponding to each process, and each flue gas purification device. The device is respectively connected to the activated carbon centralized analytical activation subsystem 2 through the activated carbon conveying subsystem 3, and the polluted activated carbon discharged from the flue gas purification device corresponding to each process is respectively transported to the total activated carbon storage tank 25 of the activated carbon centralized analytical activation subsystem 2, and then the analytical tower 23 The analysis and activation are carried out, and the activated activated carbon obtained is transported to the flue gas purification device of each step to realize the recycling of the activated carbon. The process control unit provided in the flue gas purification device in each step transmits the activated carbon circulation flow rate corresponding to the flue gas purification device to the main control unit 100, and the main control unit 100 uses the sum of the activated carbon circulation flow rates corresponding to all the processes to represent the active carbon concentration analysis activator. The activated carbon of the system 2 circulates the flow rate, and controls the activation subsystem control unit 102 disposed in the activated carbon concentration analysis activation subsystem 2 to adjust the belt scale 26, the feeding device 22, and the discharge device 24 of the activated carbon concentration analysis activation subsystem 2. Given a frequency, the activated carbon circulating flow at the activated activated carbon system 2 is substantially equal to the total activated carbon circulating flow rate of the flue gas purification device in each process, so that the adsorption portion and the analytical portion of the multi-process flue gas purification system are synchronized. The purpose is to make the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem and the activated carbon circulating flow of the flue gas purifying device of each process reach equilibrium, thereby improving the operating efficiency.
图4为本申请实施例二提供的多工序烟气净化系统的结构示意图；图5为本申请实施例二提供的多工序烟气净化系统的结构框图。4 is a schematic structural view of a multi-process flue gas purification system according to Embodiment 2 of the present application; and FIG. 5 is a structural block diagram of a multi-process flue gas purification system according to Embodiment 2 of the present application.
如图4和图5所示，本申请实施例二提供的多工序烟气净化系统，与上述实施例的区别之处在于，该系统还可应用在烧结工序中，由于在钢铁厂中，烧结工序产生的烟气要远大于其他工序产生的烟气，即烧结工序烟气产生量为钢铁厂总烟气量的70％。因此，为提高烟气净化时的运行效率，将烧结工序与活性炭集中解析活化子系统2设置在一起，即多工序烟气净化系统还包括设置于活性炭集中解析活化子系统2的烧结工序对应的烟气净化装置。As shown in FIG. 4 and FIG. 5, the multi-process flue gas purification system provided in the second embodiment of the present application is different from the above embodiment in that the system can also be applied in a sintering process due to sintering in a steel plant. The flue gas generated by the process is much larger than the flue gas produced by other processes, that is, the amount of flue gas generated in the sintering process is 70% of the total flue gas volume of the steel plant. Therefore, in order to improve the operation efficiency during the purification of the flue gas, the sintering process is set up together with the activated carbon concentration analysis activation subsystem 2, that is, the multi-process flue gas purification system further includes a sintering process disposed in the activated carbon concentration analysis activation subsystem 2 Flue gas purification device.
本实施例中，烧结工序中烟气净化装置4排放的污染活性炭无需输送至总活性炭仓25进行短暂存储，可直接输送至解析塔23中进行解析活化。In the present embodiment, the contaminated activated carbon discharged from the flue gas purification device 4 in the sintering process is not transported to the total activated carbon cartridge 25 for short-term storage, and can be directly sent to the analytical tower 23 for analytical activation.
由于烧结工序产生的烟气过多，且根据钢铁厂规模，烧结工序可包括1#烧结和2#烧结，此时，为了提高烟气净化的运行效率，可对应设置两个活性炭集中解析活化子系统2。本实施例中，仅以设置一个活性炭集中解析活化子系统2、一个烧结工序中烟气净化装置4和多个其他工序中烟气净化装置为例进行举例说明。Since the flue gas generated in the sintering process is excessive, and according to the scale of the steel plant, the sintering process may include 1# sintering and 2# sintering. At this time, in order to improve the operating efficiency of the flue gas purification, two activated carbon concentrated analytical activators may be provided correspondingly. System 2. In the present embodiment, only one activated carbon concentration analysis activation subsystem 2, one sintering process flue gas purification device 4, and a plurality of other process flue gas purification devices are exemplified.
烧结工序中烟气净化装置4与图2所示各工序的烟气净化装置的结构相同，具体地，烧结工序中烟气净化装置4包括：烧结工序给料设备41，烧结工序吸附塔42和烧结工序排料设备43。烧结工序中烟气净化装置4对烧结工序原烟气44进行烟气净化得到烧结工序净烟气45的过程与工序1烟气净化装置110相同，相应过程可参照实施例一的内容，此处不再赘述。The flue gas purification device 4 in the sintering process has the same structure as the flue gas purification device in each step shown in FIG. 2. Specifically, the flue gas purification device 4 in the sintering process includes a sintering process feeding device 41, a sintering process adsorption column 42 and Sintering process discharge device 43. In the sintering process, the flue gas purification device 4 performs the flue gas purification on the raw flue gas 44 in the sintering process to obtain the sintering process net flue gas 45. The process is the same as the flue gas purification device 110 in the first step, and the corresponding process can refer to the content of the first embodiment. No longer.
烧结工序中烟气净化装置4内设有烧结工序控制单元103，用于与主控制单元100进行双向数据传输，根据主控制单元100的指令，控制烧结工序中烟气净化装置4的工作状态及调整工作参数等。In the sintering process, the flue gas purification device 4 is provided with a sintering process control unit 103 for bidirectional data transmission with the main control unit 100, and controls the operation state of the flue gas purification device 4 in the sintering process according to the instruction of the main control unit 100. Adjust working parameters, etc.
当多工序烟气净化系统中增加烧结工序后，在计算活性炭集中解析活化子系 统的活性炭循环流量W X0时要同时考虑烧结工序中烟气净化装置4的活性炭循环流量和各工序中烟气净化装置的活性炭循环流量。 When the sintering process is added in the multi-process flue gas purification system, when calculating the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis, the activated carbon circulating flow rate of the flue gas purification device 4 in the sintering process and the flue gas purification in each process are simultaneously considered. The activated carbon circulation flow rate of the device.
在实际应用中，需要利用烧结工序控制单元103确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量W X01；将活性炭循环流量W X01发送至主控制单元100。 In practical applications, it is necessary to use the sintering process control unit 103 to determine the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process corresponding to the current time t, and to transmit the activated carbon circulation flow rate W X01 to the main control unit 100.
其中，烧结工序中烟气净化装置4的活性炭循环流量W X01，可参照上述实施例提供的方法，根据烟气中SO 2和NO X总流量来确定，此处不再赘述。 Wherein the sintering step is activated carbon gas purification apparatus of the circulation flow rate W X01 4, the above-described embodiments provide a method can be referred to, is determined according to SO 2 in the flue gas and the total flow rate of NO X, are not repeated herein.
如图9所示，烧结工序控制单元103确定出当前烟气净化装置的活性炭循环流量W X01后，将活性炭循环流量W X01发送至主控制单元100，主控制单元100按照以下步骤确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0： As shown in FIG. 9, after the sintering process control unit 103 determines the activated carbon circulation flow rate W X01 of the current flue gas purification device, the activated carbon circulation flow rate W X01 is transmitted to the main control unit 100, and the main control unit 100 determines the current time t according to the following steps. The corresponding activated carbon concentrates on the activated carbon circulation flow W X0 of the activation subsystem:
S71、确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量W X01；以及，确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间； S71, determining the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process corresponding to the current time t; and determining the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the t ni time; wherein, n The serial number of each process in the multi-process flue gas purification system; t ni = tT ni , T ni is the time when the polluted activated carbon corresponding to the flue gas purification device in process n is transported to the activated carbon centralized analytical activation subsystem at time i;
由于烧结工序与活性炭集中解析活化子系统2为一体，污染活性炭由烟气净化装置的吸附塔出口至解析塔23入口的输送时间可忽略为0，因此，获取烧结工序中烟气净化装置4的活性炭循环流量W X01的时刻可为计算活性炭集中解析活化子系统2的活性炭循环流量的当前时刻t。 Since the sintering process is integrated with the activated carbon concentration analysis activation subsystem 2, the transportation time of the contaminated activated carbon from the adsorption tower outlet of the flue gas purification device to the inlet of the analysis tower 23 can be neglected to 0, and therefore, the flue gas purification device 4 in the sintering process is obtained. The moment of the activated carbon circulation flow rate W X01 may be the current time t of calculating the activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem 2 .
工序n中烟气净化装置的活性炭循环流量W Xn(tni)的确定方法可参照上述实施例的内容，此处不再赘述。 For the method for determining the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n, reference may be made to the contents of the above embodiments, and details are not described herein again.
S72、根据工序n中烟气净化装置的活性炭循环流量W Xn(tni)和烧结工序中烟气净化装置的活性炭循环流量W X01，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； S72, according to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n and the activated carbon circulating flow W X01 of the flue gas purifying device in the sintering process, and the following formula, determining the activated carbon centralized analytical activation subsystem corresponding to the current time t Activated carbon circulation flow W X0 ;
W X0＝∑W Xn(t-Tni)+W X01。 W X0 = ∑W Xn(t-Tni)+ W X01 .
S73、根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0-W X01时对应的所述皮带秤的运行频率f c； S73, adjusting the discharge flow rate W C0 of the belt scale according to the activated carbon circulating flow rate W X0 of the activated carbon centralized analysis subsystem; and obtaining the running frequency f of the belt scale corresponding to W C =W X0 -W X01 c ;
S74、根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 S74, adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize the multi-process flue gas Control of the purification system.
此时，活性炭集中解析活化子系统2的活性炭循环流量为烧结工序中烟气净 化装置4的活性炭循环流量和各工序中烟气净化装置的活性炭循环流量之和，另外，如果多工序烟气净化系统中设有筛选活化活性炭和补充新活性炭的操作时，在计算活性炭集中解析活化子系统的活性炭循环流量时，还要考虑总活性炭仓25中补充新活性炭的补充流量W 补，进而可以保证活性炭集中解析活化子系统的理论活性炭循环流量W X0与烧结工序以及各工序中的烟气净化装置的活性炭循环流量达到平衡，从而保证整个多工序烟气净化系统能够实现同步运行，运行效率最佳。 At this time, the activated carbon circulating flow of the activated carbon concentration analysis is the sum of the activated carbon circulation flow rate of the flue gas purification device 4 in the sintering process and the activated carbon circulation flow rate of the flue gas purification device in each process, and if the multi-process flue gas purification is performed when the system is provided with activated carbon filters, and activated carbon new replenishment operation, in the calculation of focus activated charcoal activated parsing subsystem circulation rate, but also to consider the total active carbon cartridge 25 to add new makeup flow W complement activated carbon, activated carbon can ensure further The theoretical activated carbon circulation flow W X0 of the activation subsystem is concentrated and balanced with the sintering process and the activated carbon circulation flow of the flue gas purification device in each process, thereby ensuring that the entire multi-process flue gas purification system can realize synchronous operation and the operation efficiency is optimal.
当多工序烟气净化系统中增加烧结工序后，活性炭集中解析活化子系统的理论活性炭循环流量随即发生变化，且烧结工序中烟气净化装置4排放的污染活性炭直接输送至解析塔23，总活性炭仓25中仅包括其他工序排放的污染活性炭。此时，活性炭集中解析活化子系统2的理论活性炭循环流量为烧结工序中烟气净化装置4排放的活性炭循环流量与其他工序中烟气净化装置的活性炭循环流量之和。因此，为准确确定总活性炭仓25下方的皮带秤26的下料流量，需要根据活性炭集中解析活化子系统的活性炭循环流量W X0和烧结工序中烟气净化装置的活性炭循环流量W X01之差来确定。 When the sintering process is increased in the multi-process flue gas purification system, the theoretical activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem changes, and the polluted activated carbon discharged from the flue gas purification device 4 in the sintering process is directly sent to the analytical tower 23, the total activated carbon Only the polluted activated carbon discharged from other processes is included in the bin 25. At this time, the theoretical activated carbon circulation flow rate of the activated carbon concentration analysis activation subsystem 2 is the sum of the activated carbon circulation flow rate discharged by the flue gas purification device 4 in the sintering process and the activated carbon circulation flow rate of the flue gas purification device in other processes. Therefore, in order to accurately determine the discharge flow rate of the belt scale 26 below the total activated carbon cartridge 25, it is necessary to calculate the difference between the activated carbon circulation flow W X0 of the activated subsystem and the activated carbon circulation flow W X01 of the flue gas purification device in the sintering process. determine.
为此，活化子系统控制单元102被进一步配置为执行下述程序步骤：根据活性炭集中解析活化子系统的活性炭循环流量W X0和烧结工序中烟气净化装置的活性炭循环流量W X01，调整皮带秤26的下料流量W C，确定W C＝W X0-W X01时对应的皮带秤26的运行频率f c。 To this end, the activation subsystem control unit 102 is further configured to perform the following program steps: adjusting the belt scale according to the activated carbon circulation flow W X0 of the activated carbon concentration analysis activation activated carbon system and the activated carbon circulation flow rate W X01 of the flue gas purification apparatus in the sintering process The blanking flow rate W C of 26 determines the operating frequency f c of the corresponding belt scale 26 when W C = W X0 - W X01 .
当重新确定皮带秤26的运行频率f c之后，再次计算解析塔23的给料装置22的给定频率f g、排料装置24的给定频率f p与皮带秤26的运行频率f c之间的比例关系，进而根据重新确定的比例关系，调整f g、f p与f c相等，进而保证在实际运行中，皮带秤26的下料流量W C、给料装置22的下料流量W G和排料装置24的下料流量W P相等，使得活性炭集中解析活化子系统的理论活性炭循环流量W X0与各工序的烟气净化装置的活性炭循环流量达到平衡，从而保证整个多工序烟气净化系统能够实现同步运行，运行效率最佳。 After the operating frequency f c of the belt scale 26 is re-determined, the given frequency f g of the feeding device 22 of the analytical tower 23, the given frequency f p of the discharging device 24 and the operating frequency f c of the belt scale 26 are again calculated. The proportional relationship between the two, and according to the re-determined proportional relationship, adjust f g , f p and f c to be equal, thereby ensuring the unloading flow rate W C of the belt scale 26 and the discharge flow rate of the feeding device 22 in actual operation. The discharge flow rate W P of the G and the discharge device 24 is equal, so that the theoretical activated carbon circulation flow W X0 of the activated carbon centralized analysis activation subsystem and the activated carbon circulation flow rate of the flue gas purification device of each process are balanced, thereby ensuring the entire multi-process flue gas. The purification system is capable of simultaneous operation and optimum operating efficiency.
需要说明的是，f g、f p与f c的比例关系的确定方式，可参照实施例一提供的相应方法，此处不再赘述。 It should be noted that the method for determining the proportional relationship between f g , f p and f c can be referred to the corresponding method provided in the first embodiment, and details are not described herein again.
由于本实施例提供的多工序烟气净化系统中包括烧结工序对应的烟气净化装置，以及其他各工序对应的烟气净化装置，在产生活化活性炭之后，存在为钢铁厂内各工序分配相应量的活性炭的问题。且烧结工序中产生的烟气量要远大于其他各工序产生的烟气量，因此，为了保证烧结工序中烟气净化装置的最佳吸附效果，需要为烧结工序分配较多的活化活性炭，该分配量需要根据相应烟气净化 装置的吸附塔的装填量或者烧结工序对应的活性炭循环流量进行确定，而分配给其他工序的活性炭量即为分配给烧结工序后余下的所有活性炭。Since the multi-process flue gas purification system provided in the embodiment includes the flue gas purifying device corresponding to the sintering process and the flue gas purifying device corresponding to the other processes, after the activated activated carbon is generated, there is a corresponding amount allocated for each process in the steel plant. The problem with activated carbon. Moreover, the amount of flue gas generated in the sintering process is much larger than the amount of flue gas generated in the other processes. Therefore, in order to ensure the optimal adsorption effect of the flue gas purification device in the sintering process, it is necessary to allocate a large amount of activated activated carbon to the sintering process. The amount of distribution needs to be determined according to the loading amount of the adsorption tower of the corresponding flue gas purification device or the circulating flow rate of the activated carbon corresponding to the sintering process, and the amount of activated carbon distributed to other processes is all the activated carbon remaining after being distributed to the sintering process.
因此，为实现活化活性炭的准确分配，以使多工序烟气净化系统维持平衡的循环状态，需要采用分料装置20进行按需分配活化活性炭。Therefore, in order to achieve accurate distribution of activated activated carbon, so that the multi-process flue gas purification system maintains a balanced circulation state, it is necessary to use the dispensing device 20 to perform on-demand distribution of activated activated carbon.
本实施例中，活性炭集中解析活化子系统2还包括位于活化活性炭仓28下方的分料装置20；分料装置20包括用于为各工序分配活化活性炭的工序卸料装置202，以及用于为烧结工序分配活化活性炭的烧结工序卸料装置201。In this embodiment, the activated carbon concentration analysis activation subsystem 2 further includes a dispensing device 20 located below the activated activated carbon cartridge 28; the dispensing device 20 includes a process unloading device 202 for dispensing activated carbon for each process, and for In the sintering step, the unloading device 201 for activating the activated carbon is distributed.
首先利用烧结工序卸料装置201为钢铁厂内烧结工序中烟气净化装置4分配活性炭，分配的活性炭量根据相应烟气净化装置中吸附塔的装填量或者烧结工序对应的活性炭循环流量来确定。First, the activated carbon is distributed to the flue gas purification device 4 in the sintering process in the steel plant by the sintering process unloading device 201, and the amount of activated carbon to be distributed is determined according to the loading amount of the adsorption tower in the corresponding flue gas purification device or the circulating flow rate of the activated carbon corresponding to the sintering process.
在其中一种具体的实施方式中，烧结工序分配的活性炭量根据相应烟气净化装置中吸附塔的装填量来确定。In one specific embodiment, the amount of activated carbon dispensed in the sintering process is determined according to the loading amount of the adsorption column in the corresponding flue gas cleaning device.
本实施例中，烧结工序烟气净化装置中吸附塔的装填量Q 烧0按照下式确定：Q 烧0＝W X01×T 烧0； In this embodiment, the sintering process the amount of flue gas cleaning apparatus of the adsorption tower charged firing Q 0 determined according to the following formula: Q burning 0 = W X01 × T 0 burn;
式中，Q 烧0为烧结工序中吸附塔内活性炭的装填量，单位kg；W X01为烧结工序中烟气净化装置在当前时刻t的活性炭循环流量，单位kg/h；T 烧0为烧结工序中吸附塔内活性炭的停留时间，取值范围为110～170，单位h；其中，停留时间T 烧0根据烟气量、烟气流速等确定。 In the formula, Q- burning 0 is the loading amount of activated carbon in the adsorption tower in the sintering process, unit kg; W X01 is the circulating flow rate of activated carbon at the current time t in the sintering process in the sintering process, unit kg/h; T- burning is sintering activated carbon adsorption tower step the residence time in the range of 110 to 170, H units; wherein the residence time T 0 determined according to burn gas volume, gas velocity and the like.
确定出烧结工序对应的烟气净化装置的吸附塔的装填量后，即可确定烧结工序卸料装置的总卸料量，进而可确定单位时间内烧结工序卸料装置201的卸料流量W 卸1。 After determining the loading amount of the adsorption tower of the flue gas purification device corresponding to the sintering process, the total discharge amount of the unloading device in the sintering process can be determined, and the discharge flow rate unloading of the unloading device 201 in the sintering process per unit time can be determined. 1 .
在另一种具体的实施方式中，烧结工序分配的活性炭量根据烧结工序对应的活性炭循环流量来确定。In another specific embodiment, the amount of activated carbon dispensed in the sintering step is determined according to the circulating flow rate of activated carbon corresponding to the sintering step.
由于吸附塔排出的活性炭吸附有污染物，所以同样体积的活性炭，重量会增加3％～10％，即同一批活性炭，解析活化后的重量为吸附污染物后重量的0.9～0.97，因此，在确定烧结工序中烟气净化装置4对应的理论活性炭循环流量时，要考虑重量的变化系数j，即烧结工序卸料装置201的卸料流量W 卸1按照下式确定： Since the activated carbon discharged from the adsorption tower adsorbs pollutants, the weight of the activated carbon of the same volume will increase by 3% to 10%, that is, the same batch of activated carbon, and the weight after the analytical activation is 0.9 to 0.97 after the adsorption of the pollutant, therefore, When determining the theoretical activated carbon circulation flow rate corresponding to the flue gas purification device 4 in the sintering process, the coefficient of variation j of the weight, that is, the discharge flow rate W of the unloading device 201 of the sintering process, is determined as follows:
W 卸1＝W X01×j； W unload 1 = W X01 × j;
式中，j为系数，取值范围为0.9～0.97。In the formula, j is a coefficient, and the value ranges from 0.9 to 0.97.
当确定出烧结工序卸料装置201的卸料流量后，实际上，其他各工序的卸料 流量W 卸2为活性炭集中解析活化子系统的理论活性炭循环流量W X0与烧结工序卸料装置201的卸料流量W 卸1之差，但为了保证多工序烟气净化系统的连续运行，提高运行效率，本实施例中，将为其他各工序中烟气净化装置分配活性炭的工序卸料装置202的卸料流量W 卸2设置为最大，以实现分料装置中存储多少料就运输多少料的目的。 When the sintering step is determined that the discharge flow rate of the discharging device 201 is, in fact, the discharge flow rate of each other unloading step W 2 concentration of the Theory of activated charcoal circulation flow rate W and the sintering step X0 discharge means activated subsystem 201 difference between the discharge flow rate W 1 discharged, but in order to ensure continuous operation of a multi-step flue gas purification system, and improve operational efficiency, in this embodiment, the step apparatus for dispensing the activated carbon each other flue gas cleaning process, the discharge device 202 The discharge flow W unloading 2 is set to the maximum to achieve the purpose of transporting how much material is stored in the material distribution device.
在第三种实施例中，还可在实施例二提供的多工序烟气净化系统中配置新活性炭补充装置29，具体地，如图10所示，主控制单元100被配置为执行下述步骤，以实现对多工序烟气净化系统的精准控制：In the third embodiment, the new activated carbon replenishing device 29 can also be configured in the multi-process flue gas purification system provided in the second embodiment. Specifically, as shown in FIG. 10, the main control unit 100 is configured to perform the following steps. To achieve precise control of multi-process flue gas purification systems:
S81、确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量W X01，确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)；以及，确定新活性炭补充装置的补充新活性炭的补充流量W 补；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间； S81, determining the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process corresponding to the current time t, determining the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the t ni time; and determining the new activated carbon add new activated carbon added up device makeup flow W; where, n is a multi-step gas purification system number of each step; t ni = tT ni, T ni of the flue gas cleaning device step n at time i corresponds to contamination The time when the activated carbon is transported to the activated carbon to analyze the activation subsystem;
S82、根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)、烧结工序中烟气净化装置的活性炭循环流量W X01和补充流量W 补，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； S82, according to the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n, the activated carbon circulation flow rate W X01 and the supplementary flow rate W supplement of the flue gas purification device in the sintering process, and the following formula, determining the current time t corresponding The activated carbon concentrates on the activated carbon circulation flow W X0 of the activation subsystem;
W X0＝∑W Xn(t-Tni)+W 补+W X01； W X0 = ∑W Xn(t-Tni)+ W complement + W X01 ;
S83、根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0-W X01时对应的所述皮带秤的运行频率f c； S83, based on the activated charcoal parsing subsystem centralized charcoal circulation flow rate W X0, adjusting the feed flow rate of the belt weigher W C; and obtaining W C = W X0 -W X01 corresponding to when the belt scale operating frequency f c ;
S84、根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 S84, adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize multi-process flue gas Control of the purification system.
本实施例提供的多工序烟气净化系统，其具体的实现过程可相应参照实施例一和实施例二的对应部分内容，此处不再赘述。For the specific implementation process of the multi-process flue gas purification system provided in this embodiment, reference may be made to the corresponding parts of the first embodiment and the second embodiment, and details are not described herein again.
本实施例提供的多工序烟气净化系统，将产生较多烟气的烧结工序与活性炭集中解析活化子系统设置在一起，烧结工序中烟气净化装置4排放的污染活性炭能够以最快的速度进入活性炭集中解析活化子系统2进行解析活化，避免在输送途中浪费时间，造成系统运行效率降低。而在根据活性炭集中解析活化子系统2的活性炭循环流量控制整个系统的运行参数时，充分考虑烧结工序对应的活性炭循环流量和其他各工序对应的活性炭循环流量，使得在控制解析塔的给料装置22的给定频率f g、排料装置24的给定频率f p与皮带秤26的运行频率f c相等时的数 据准确，以保证活性炭集中解析活化子系统的活性炭循环流量W X0与烧结工序及其他各工序对应的烟气净化装置的活性炭循环流量达到平衡，从而保证整个多工序烟气净化系统能够实现同步、平稳运行，运行效率最佳。 The multi-process flue gas purification system provided in this embodiment sets the sintering process for generating more flue gas together with the activated carbon centralized analytical activation subsystem, and the polluted activated carbon discharged from the flue gas purification device 4 in the sintering process can be at the fastest speed. Entering the activated carbon centralized analysis activation subsystem 2 for analytical activation, avoiding wasting time during transportation, resulting in reduced system operating efficiency. When the operating parameters of the activated carbon of the activation subsystem 2 are analyzed according to the activated carbon concentration, the circulation flow rate of the activated carbon corresponding to the sintering process and the circulating flow rate of the activated carbon corresponding to the other processes are fully considered, so that the feeding device for controlling the analytical tower is controlled. The given frequency f g of 22, the given frequency f p of the discharge device 24 and the operating frequency f c of the belt scale 26 are equal, so as to ensure that the activated carbon concentrates on the activated carbon circulation flow W X0 and the sintering process. And the circulation flow rate of the activated carbon corresponding to the flue gas purification device corresponding to each process is balanced, thereby ensuring that the entire multi-process flue gas purification system can achieve synchronous and smooth operation, and the operation efficiency is optimal.
根据上述实施例提供的多工序烟气净化系统，如图6所示，本申请实施例提供一种多工序烟气净化系统的控制方法，应用于上述实施例提供的多工序烟气净化系统，该控制方法包括以下步骤：According to the multi-process flue gas purification system provided by the above embodiment, as shown in FIG. 6, the embodiment of the present application provides a multi-process flue gas purification system control method, which is applied to the multi-process flue gas purification system provided by the above embodiment. The control method includes the following steps:
S1、确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间； S1, determining the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the time t ni ; wherein n is the serial number of each step in the multi-process flue gas purification system; t ni =tT ni , T ni is In the process n, the flue gas purification device transports the contaminated activated carbon corresponding to the time of i to the time when the activated carbon is concentrated to analyze the activation subsystem;
S2、根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； S2, according to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the process n, determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
S3、根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0时对应的所述皮带秤的运行频率f c； S3, adjusting the flow rate W C0 of the belt scale according to the activated carbon circulating flow W X0 of the activated carbon centralized analysis subsystem; and obtaining the running frequency f c of the belt scale corresponding to W C = W X0 ;
S4、根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 S4, adjusting a given frequency f g of the feeding device in the activated carbon centralized resolution activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize multi-process flue gas Control of the purification system.
可选地，如图7所示，按照以下步骤确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)： Optionally, as shown in FIG. 7, the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the time t ni is determined according to the following steps:
S21、根据工序n在生产过程中产生的原烟气总量V n，以及根据下式，计算t ni时刻对应的所述原烟气中的SO 2和NO X总流量； S21, according to step n generated in the production process of the original total amount of flue gas V n, and SO 2 and NO X in accordance with the total flow rate of the original flue t ni time corresponding to the following formula, is calculated;
W Sn(tni)＝V n×C Sn/10 6； W Sn(tni) = V n × C Sn /10 6 ;
W Nn(tni)＝V n×C Nn/10 6； W Nn(tni) = V n × C Nn /10 6 ;
式中，W Sn(tni)为工序n在t ni时刻对应的原烟气中的SO 2总流量，单位kg/h；W Nn(tni)为工序n在t ni时刻对应的原烟气中的NO X总流量，单位kg/h；C Sn为工序n在t ni时刻对应的原烟气中的SO 2浓度，单位mg/Nm 3；C Nn为工序n在t ni时刻对应的原烟气中的NO X浓度，单位mg/Nm 3； Where W Sn(tni) is the total flow rate of SO 2 in the raw flue gas corresponding to the step n at time t ni , in units of kg/h; W Nn(tni) is the original flue gas corresponding to the step n at time t ni the total NO X flow rate, the unit kg / h; 2 C Sn concentration of SO original flue step n at time t ni corresponding to the units mg / Nm 3; C Nn to step n at time t ni corresponding raw tobacco NO X in the gas concentration, the unit mg / Nm 3;
S22、根据所述原烟气中的SO 2和NO X总流量，以及下式，计算t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)； S22, according to SO 2 X and the total flow of the raw flue gas NO, and the following equation, calculated t ni corresponding to the time step n flue gas purification device activated circulation flow rate W Xn (tni);
W Xn(tni)＝K 1×W Sn(tni)+K 2×W Nn(tni)； W Xn(tni) = K 1 × W Sn(tni) + K 2 × W Nn(tni) ;
式中，W Xn(tni)为工序n中烟气净化装置对应的t ni时刻的活性炭循环流量，单位kg/h；K 1为第一系数，取值范围为15～21；K 2为第二系数，取值范围为3～5。 In the formula, W Xn(tni) is the circulating flow rate of activated carbon at t ni time corresponding to the flue gas purification device in process n, unit kg/h; K 1 is the first coefficient, and the value ranges from 15 to 21; K 2 is the first The two coefficients are in the range of 3 to 5.
可选地，所述确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0的步骤包括： Optionally, the step of determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t includes:
按照下式，根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； According to the following formula, according to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n, the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t is determined;
W X0＝∑W Xn(tni)＝∑W Xn(t-Tni)； W X0 = ∑W Xn(tni)= ∑W Xn(t-Tni) ;
式中，t为当前时刻，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间。 In the formula, t is the current time, and T ni is the time during which the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon concentration analysis activation subsystem.
可选地，按照以下步骤确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0： Optionally, the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t is determined according to the following steps:
确定所述新活性炭补充装置的补充新活性炭的补充流量W 补，以根据所述补充流量W 补，控制所述新活性炭补充装置向总活性炭仓内补充新活性炭； Determining the new supplemental active carbon replenishing device makeup flow GAC complement of W, W to fill in accordance with the makeup flow, the control GAC GAC supply apparatus into the total activated carbon cartridge;
根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)，补充流量W 补，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； According to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the step n, the supplementary flow rate W complement , and the following formula, determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
W X0＝∑W Xn(t-Tni)+W 补。 W X0 = ∑W Xn(t-Tni) +W complement .
可选地，如图8所示，按照以下步骤确定所述新活性炭补充装置的补充新活性炭的补充流量W 补： Alternatively, as shown in FIG. 8, the following step of determining the supplementary replenishing apparatus GAC GAC supplementary flow rate W Complement:
根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，按照下式，确定活性炭集中解析活化子系统中解析塔的活性炭装填料量Q 0； According to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem, according to the following formula, the activated carbon loading amount Q 0 of the analytical tower in the activated carbon centralized analytical activation subsystem is determined;
Q 0＝W X0×T 0； Q 0 = W X0 × T 0 ;
式中，Q 0为活性炭集中解析活化子系统中解析塔的活性炭装填料量，单位kg；T 0为解析塔内活性炭的停留时间，取值范围4～8，单位h； Wherein, Q 0 is the activated carbon loading amount of the analytical tower in the activated carbon concentration analysis activation subsystem, unit kg; T 0 is the residence time of the activated carbon in the analytical tower, the value ranges from 4 to 8, unit h;
检测所述活性炭集中解析活化子系统中活化活性炭仓的实际活性炭料量Q 实； Detecting the actual charcoal activated charcoal concentrated parsing subsystem quantity Q of the solid activated carbon cartridge;
根据所述解析塔的活性炭装填料量Q 0和实际活性炭料量Q 实，按照式Q 损＝Q 0-Q 实，确定活性炭经所述筛分装置筛分处理后的损耗活性炭料量Q 损； According to the analysis of activated carbon packed column quantity Q 0 of the activated carbon and the actual real quantity Q, in accordance with the formula Q = Q 0 -Q real loss, determine the loss quantity Q activated charcoal loss after sieving through the sieve processing means ;
控制所述新活性炭补充装置的补充活性炭料量Q 补与损耗活性炭料量Q 损相等，根据调整后的补充活性炭料量Q 补，确定单位时间的新活性炭补充装置的补充新活性炭的补充流量W 补。 Controlling said supplementary GAC GAC supplementary replenishing device activated charcoal loss quantity Q and complement loss quantity Q is equal to, activated carbon supplementary quantity Q adjusted up, new activated carbon per unit time determines supplementary device makeup flow W Make up .
可选地，按照下述步骤根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p： Optionally, the given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and the given frequency f p of the discharging device are adjusted according to the operating frequency f c of the belt weigher according to the following steps:
确定所述皮带秤的下料流量W C＝K c×f c，给料装置的下料流量W G＝K g×f g，排料装置的下料流量W P＝K p×f p；式中，Kc、K g和K p均为常数； Determining the discharge flow rate of the belt weigher W C = K c × f c , the discharge flow rate of the feeding device W G = K g × f g , the discharge flow rate of the discharge device W P = K p × f p ; Where Kc, K g and K p are constants;
控制所述活性炭集中解析活化子系统的给料装置、排料装置和皮带秤的下料流量相同，使得W G＝W P＝W C＝W X0； The feeding flow rate of the feeding device, the discharging device and the belt weigher for controlling the activated carbon centralized analytical activation subsystem is the same, so that W G = W P = W C = W X0 ;
根据上式，得到所述给料装置的给定频率f g与皮带秤的运行频率f c之间满足下式关系：
Figure PCTCN2018083579-appb-000005
以根据上式及皮带秤的运行频率f c，调整给料装置的给定频率f g；以及， According to the above formula, the relationship between the given frequency f g of the feeding device and the operating frequency f c of the belt weigher is obtained:
Figure PCTCN2018083579-appb-000005
Adjusting the given frequency f g of the feeding device according to the above formula and the operating frequency f c of the belt weigher;
得到所述排料装置的给定频率f p与皮带秤的运行频率f c之间满足下式关系：
Figure PCTCN2018083579-appb-000006
以根据上式及皮带秤的运行频率f c，调整排料装置的给定频率f p。 Obtaining the following relationship between the given frequency f p of the discharge device and the operating frequency f c of the belt scale:
Figure PCTCN2018083579-appb-000006
The given frequency f p of the discharge device is adjusted according to the above formula and the operating frequency f c of the belt weigher.
第三方面，根据上述实施例提供的多工序烟气净化系统，如图9所示，本申请实施例提供一种多工序烟气净化系统的控制方法，应用于上述实施例提供的多工序烟气净化系统，该控制方法包括以下步骤：In a third aspect, according to the multi-process flue gas purification system provided in the above embodiment, as shown in FIG. 9 , the embodiment of the present application provides a control method for a multi-process flue gas purification system, which is applied to the multi-process smoke provided by the above embodiment. The gas purification system, the control method comprises the following steps:
S71、确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量W X01；以及，确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间； S71, determining the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process corresponding to the current time t; and determining the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the t ni time; wherein, n The serial number of each process in the multi-process flue gas purification system; t ni = tT ni , T ni is the time when the polluted activated carbon corresponding to the flue gas purification device in process n is transported to the activated carbon centralized analytical activation subsystem at time i;
S72、根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)和烧结工序中烟气净化装置的活性炭循环流量W X01，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； S72, determining, according to the activated carbon circulating flow rate W Xn(tni) of the flue gas purifying device in the process n and the activated carbon circulating flow rate W X01 of the flue gas purifying device in the sintering process, and the following formula, determining the concentrated analytical activation of the activated carbon corresponding to the current time t The activated carbon circulation flow of the subsystem W X0 ;
W X0＝∑W Xn(t-Tni)+W X01； W X0 = ∑W Xn(t-Tni) +W X01 ;
S73、根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0-W X01时对应的所述皮带秤的运行频率f c； S73, adjusting the discharge flow rate W C0 of the belt scale according to the activated carbon circulating flow rate W X0 of the activated carbon centralized analysis subsystem; and obtaining the running frequency f of the belt scale corresponding to W C =W X0 -W X01 c ;
S74、根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 S74, adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize the multi-process flue gas Control of the purification system.
可选地，还包括：Optionally, it also includes:
根据所述烧结工序中烟气净化装置的活性炭循环流量W X01，以及式W 卸1＝W X01×j，确定烧结工序卸料装置的卸料流量W 卸1；其中，j为系数，取值范围为0.9～0.97；以及，控制所述工序n卸料装置的卸料流量W 卸2为最大。 According to the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process, and the formula W unloading 1 = W X01 × j, the unloading flow rate W of the unloading device in the sintering process is determined to be unloaded ; wherein j is a coefficient, and the value is The range is from 0.9 to 0.97; and the discharge flow rate W of the unloading device of the process n is controlled to be the maximum.
第四方面，根据上述实施例提供的多工序烟气净化系统，如图10所示，本申请实施例提供一种多工序烟气净化系统的控制方法，应用于上述实施例提供的多工序烟气净化系统，该控制方法包括以下步骤：In a fourth aspect, according to the multi-process flue gas purification system provided in the above embodiment, as shown in FIG. 10, the embodiment of the present application provides a multi-process flue gas purification system control method, which is applied to the multi-process smoke provided by the above embodiment. The gas purification system, the control method comprises the following steps:
S81、确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量W X01，确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量W Xn(tni)；以及，确定新活性炭补充装置的补充新活性炭的补充流量W 补；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间； S81, determining the activated carbon circulation flow rate W X01 of the flue gas purification device in the sintering process corresponding to the current time t, determining the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n corresponding to the t ni time; and determining the new activated carbon add new activated carbon added up device makeup flow W; where, n is a multi-step gas purification system number of each step; t ni = tT ni, T ni of the flue gas cleaning device step n at time i corresponds to contamination The time when the activated carbon is transported to the activated carbon to analyze the activation subsystem;
S82、根据所述工序n中烟气净化装置的活性炭循环流量W Xn(tni)、烧结工序中烟气净化装置的活性炭循环流量W X01和补充流量W 补，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0； S82, according to the activated carbon circulation flow rate W Xn(tni) of the flue gas purification device in the step n, the activated carbon circulation flow rate W X01 and the supplementary flow rate W supplement of the flue gas purification device in the sintering process, and the following formula, determining the current time t corresponding The activated carbon concentrates on the activated carbon circulation flow W X0 of the activation subsystem;
W X0＝∑W Xn(t-Tni)+W 补+W X01； W X0 = ∑W Xn(t-Tni)+ W complement + W X01 ;
S83、根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0-W X01时对应的所述皮带秤的运行频率f c； S83, based on the activated charcoal parsing subsystem centralized charcoal circulation flow rate W X0, adjusting the feed flow rate of the belt weigher W C; and obtaining W C = W X0 -W X01 corresponding to when the belt scale operating frequency f c ;
S84、根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 S84, adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize multi-process flue gas Control of the purification system.
具体实现中，本发明还提供一种计算机存储介质，其中，该计算机存储介质可存储有程序，该程序执行时可包括本发明提供的多工序烟气净化系统的控制方法的各实施例中的部分或全部步骤。所述的存储介质可为磁碟、光盘、只读存储记忆体(英文：read-only memory，简称：ROM)或随机存储记忆体(英文：random access memory，简称：RAM)等。In a specific implementation, the present invention further provides a computer storage medium, wherein the computer storage medium may store a program, where the program may be executed in the embodiments of the control method of the multi-process flue gas purification system provided by the present invention. Some or all of the steps. The storage medium may be a magnetic disk, an optical disk, a read-only memory (English: read-only memory, abbreviated as: ROM) or a random access memory (English: random access memory, abbreviation: RAM).
本领域的技术人员可以清楚地了解到本发明实施例中的技术可借助软件加必需的通用硬件平台的方式来实现。基于这样的理解，本发明实施例中的技术方案本质上或者说对现有技术做出贡献的部分可以以软件产品的形式体现出来，该计算机软件产品可以存储在存储介质中，如ROM/RAM、磁碟、光盘等，包括若干指令用以使得一台计算机设备(可以是个人计算机，服务器，或者网络设备等)执行本发明各个实施例或者实施例的某些部分所述的方法。It will be apparent to those skilled in the art that the techniques in the embodiments of the present invention can be implemented by means of software plus a necessary general hardware platform. Based on such understanding, the technical solution in the embodiments of the present invention may be embodied in the form of a software product in essence or in the form of a software product, which may be stored in a storage medium such as a ROM/RAM. , a disk, an optical disk, etc., including instructions for causing a computer device (which may be a personal computer, server, or network device, etc.) to perform the methods described in various embodiments of the present invention or portions of the embodiments.
本说明书中各个实施例之间相同相似的部分互相参见即可。尤其，对于多工序烟气净化系统的控制方法实施例而言，由于其基本相似于多工序烟气净化系统实施例，所以描述的比较简单，相关之处参见多工序烟气净化系统实施例中的说明即可。The same and similar parts between the various embodiments in this specification can be referred to each other. In particular, for the control method embodiment of the multi-process flue gas purification system, since it is basically similar to the multi-process flue gas purification system embodiment, the description is relatively simple, and the relevant points are referred to the multi-process flue gas purification system embodiment. The instructions are fine.
以上所述的本发明实施方式并不构成对本发明保护范围的限定。The embodiments of the invention described above are not intended to limit the scope of the invention.

Claims (11)

  1. 一种多工序烟气净化系统，其特征在于，包括：活性炭集中解析活化子系统，活性炭输送子系统，以及与各工序对应的烟气净化装置，每一所述烟气净化装置分别通过活性炭输送子系统与活性炭集中解析活化子系统连接；其中，A multi-process flue gas purification system, comprising: an activated carbon concentration analysis activation subsystem, an activated carbon transportation subsystem, and a flue gas purification device corresponding to each process, each of the flue gas purification devices respectively being transported by activated carbon The subsystem is connected to the activated carbon centralized analytical activation subsystem; wherein
    所述活性炭集中解析活化子系统包括解析塔，用于控制进入解析塔内污染活性炭流量的给料装置，用于将解析塔内经过活化处理后的活化活性炭排出的排料装置，用于对所述排料装置排出的活化活性炭进行筛分的筛分装置，用于收集经筛分装置后得到的活化活性炭的活化活性炭仓，设置在各工序对应的烟气净化装置的出口端与给料装置之间的总活性炭仓，所述总活性炭仓用于收集各工序中烟气净化装置排放的污染活性炭，设置在所述总活性炭仓与给料装置之间的皮带秤，所述皮带秤用于将总活性炭仓内的污染活性炭输送至解析塔，以及，设置在总活性炭仓上方的新活性炭补充装置，所述新活性炭补充装置用于向总活性炭仓内补充新活性炭。The activated carbon centralized analytical activation subsystem comprises an analytical tower, a feeding device for controlling the flow rate of the contaminated activated carbon entering the analytical tower, and a discharging device for discharging the activated activated carbon in the analytical tower after the activation treatment, for the purpose of a screening device for screening activated activated carbon discharged from a discharge device for collecting activated activated carbon activated carbon obtained by the screening device, and providing an outlet end of the flue gas purification device corresponding to each process and a feeding device a total activated carbon cartridge between the total activated carbon cartridge for collecting the polluted activated carbon discharged from the flue gas purification device in each process, and a belt scale disposed between the total activated carbon cartridge and the feeding device, the belt scale being used for The contaminated activated carbon in the total activated carbon storage tank is sent to the analytical tower, and a new activated carbon replenishing device is disposed above the total activated carbon storage tank, and the new activated carbon replenishing device is used to replenish the activated carbon in the total activated carbon storage tank.
  2. 根据权利要求1所述的系统，其特征在于，还包括：设置于所述活性炭集中解析活化子系统的烧结工序对应的烟气净化装置，以及，位于活化活性炭仓下方的分料装置；所述烧结工序对应的烟气净化装置排放的污染活性炭通过活性炭输送子系统以及给料装置送入解析塔；The system according to claim 1, further comprising: a flue gas purification device corresponding to a sintering process of the activated carbon concentration analysis activation subsystem, and a dosing device located below the activated activated carbon cartridge; The polluted activated carbon discharged from the flue gas purification device corresponding to the sintering process is sent to the analytical tower through the activated carbon conveying subsystem and the feeding device;
    所述分料装置包括用于为各工序分配活化活性炭的工序n卸料装置，以及用于为烧结工序分配活化活性炭的烧结工序卸料装置。The materializing device includes a step n discharging device for distributing activated carbon for each step, and a sintering step discharging device for distributing activated carbon for the sintering step.
  3. 一种多工序烟气净化系统的控制方法，其特征在于，包括以下步骤：A method for controlling a multi-process flue gas purification system, comprising the steps of:
    确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100001
    其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间；     Determine the activated carbon circulation flow rate of the flue gas purification device in the process n corresponding to the time t ni
    Figure PCTCN2018083579-appb-100001
    Where n is the serial number of each step in the multi-process flue gas purification system; t ni = tT ni , T ni is the time during which the flue gas purification device corresponding to the flue gas purification device in step n is transported to the activated carbon centralized analytical activation subsystem at time i;
    根据所述工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100002
    确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0；     According to the activated carbon circulation flow rate of the flue gas purification device in the process n
    Figure PCTCN2018083579-appb-100002
    Determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
    根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取W C＝W X0时对应的所述皮带秤的运行频率f c； Adjusting the blanking flow rate W C of the belt scale according to the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem; and obtaining the operating frequency f c of the belt scale corresponding to W C = W X0 ;
    根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 Adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize the multi-process flue gas purification system control.
  4. 根据权利要求3所述的方法，其特征在于，按照下述步骤确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100003
    The method according to claim 3, characterized in that the activated carbon circulation flow rate of the flue gas purification device in the process n corresponding to the time t ni is determined according to the following steps
    Figure PCTCN2018083579-appb-100003
    根据工序n在生产过程中产生的原烟气总量V n，以及根据下式，计算t ni时刻对应的所述原烟气中的SO 2和NO X总流量； The step n generated in the production process of the original total amount of flue gas V n, and SO 2 and NO X in accordance with the total flow rate of the original flue t ni time corresponding to the following formula, is calculated;
    Figure PCTCN2018083579-appb-100004
    Figure PCTCN2018083579-appb-100004
    Figure PCTCN2018083579-appb-100005
    Figure PCTCN2018083579-appb-100005
    式中，
    Figure PCTCN2018083579-appb-100006
    为工序n在t ni时刻对应的原烟气中的SO 2总流量，单位kg/h；
    Figure PCTCN2018083579-appb-100007
    为工序n在t ni时刻对应的原烟气中的NO X总流量，单位kg/h；
    Figure PCTCN2018083579-appb-100008
    为工序n在t ni时刻对应的原烟气中的SO 2浓度，单位mg/Nm 3；
    Figure PCTCN2018083579-appb-100009
    为工序n在t ni时刻对应的原烟气中的NO X浓度，单位mg/Nm 3；     In the formula,
    Figure PCTCN2018083579-appb-100006
    The total flow rate of SO 2 in the raw flue gas corresponding to the process n at t ni , in units of kg/h;
    Figure PCTCN2018083579-appb-100007
    NO X flow rate of the total original flue step n at time t ni corresponding to the unit kg / h;
    Figure PCTCN2018083579-appb-100008
    The concentration of SO 2 in the raw flue gas corresponding to the step n at time t ni , in units of mg/Nm 3 ;
    Figure PCTCN2018083579-appb-100009
    NO X concentration to original flue step n at time t ni corresponding to the units mg / Nm 3;
    根据所述原烟气中的SO 2和NO X总流量，以及下式，计算t ni时刻对应的工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100010
    According to the original flue gas SO 2 and NO X total flow, and the following equation, the circulation flow rate is calculated charcoal t ni corresponding to the time step n in the flue gas cleaning device
    Figure PCTCN2018083579-appb-100010
    Figure PCTCN2018083579-appb-100011
    Figure PCTCN2018083579-appb-100011
    式中，
    Figure PCTCN2018083579-appb-100012
    为工序n中烟气净化装置对应的t ni时刻的活性炭循环流量，单位kg/h；K 1为第一系数，取值范围为15～21；K 2为第二系数，取值范围为3～5。     In the formula,
    Figure PCTCN2018083579-appb-100012
    It is the circulation flow rate of activated carbon at t ni time corresponding to the flue gas purification device in process n, unit kg/h; K 1 is the first coefficient, the value ranges from 15 to 21; K 2 is the second coefficient, and the value ranges from 3 ~5.
  5. 根据权利要求3所述的方法，其特征在于，按照下述步骤确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0： The method according to claim 3, characterized in that the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t is determined according to the following steps:
    按照下式，根据所述工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100013
    确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0；     According to the following formula, according to the activated carbon circulation flow rate of the flue gas purification device in the process n
    Figure PCTCN2018083579-appb-100013
    Determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
    Figure PCTCN2018083579-appb-100014
    Figure PCTCN2018083579-appb-100014
    式中，t为当前时刻，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间。 In the formula, t is the current time, and T ni is the time during which the polluted activated carbon corresponding to the flue gas purification device in step n is transported to the activated carbon concentration analysis activation subsystem.
  6. 根据权利要求3所述的方法，其特征在于，按照下述步骤确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0： The method according to claim 3, characterized in that the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t is determined according to the following steps:
    确定新活性炭补充装置的补充新活性炭的补充流量W 补，以根据所述补充流量W 补，控制所述新活性炭补充装置向总活性炭仓内补充新活性炭； Determining supplementary replenishing device GAC GAC supplemental traffic complement of W, W to fill in accordance with the makeup flow, the control GAC GAC supply apparatus into the total activated carbon cartridge;
    根据所述工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100015
    补充流量W 补，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0；     According to the activated carbon circulation flow rate of the flue gas purification device in the process n
    Figure PCTCN2018083579-appb-100015
    The supplementary flow W complement , and the following formula, determine the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem corresponding to the current time t;
    Figure PCTCN2018083579-appb-100016
    Figure PCTCN2018083579-appb-100016
  7. 根据权利要求6所述的方法，其特征在于，按照下述步骤确定新活性炭补充装置的补充新活性炭的补充流量W 补： The method according to claim 6, wherein the step of determining according to the following supplementary replenishing apparatus GAC GAC supplementary flow rate W Complement:
    根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，按照下式，确定活性炭集中解析活化子系统中解析塔的活性炭装填料量Q 0； According to the activated carbon circulating flow rate W X0 of the activated carbon concentration analysis activation subsystem, according to the following formula, the activated carbon loading amount Q 0 of the analytical tower in the activated carbon centralized analytical activation subsystem is determined;
    Figure PCTCN2018083579-appb-100017
    Figure PCTCN2018083579-appb-100017
    式中，Q 0为活性炭集中解析活化子系统中解析塔的活性炭装填料量，单位kg；T 0为解析塔内活性炭的停留时间，取值范围4～8，单位h； Wherein, Q 0 is the activated carbon loading amount of the analytical tower in the activated carbon concentration analysis activation subsystem, unit kg; T 0 is the residence time of the activated carbon in the analytical tower, the value ranges from 4 to 8, unit h;
    检测所述活性炭集中解析活化子系统中活化活性炭仓的实际活性炭料量Q 实； Detecting the actual charcoal activated charcoal concentrated parsing subsystem quantity Q of the solid activated carbon cartridge;
    根据所述解析塔的活性炭装填料量Q 0和实际活性炭料量Q 实，按照式Q 损＝Q 0-Q 实，确定活性炭经所述筛分装置筛分处理后的损耗活性炭料量Q 损； According to the analysis of activated carbon packed column quantity Q 0 of the activated carbon and the actual real quantity Q, in accordance with the formula Q = Q 0 -Q real loss, determine the loss quantity Q activated charcoal loss after sieving through the sieve processing means ;
    控制所述新活性炭补充装置的补充活性炭料量Q 补与损耗活性炭料量Q 损相等，根据调整后的补充活性炭料量Q 补，确定单位时间的新活性炭补充装置的补充新活性炭的补充流量W 补。 Controlling said supplementary GAC GAC supplementary replenishing device activated charcoal loss quantity Q and complement loss quantity Q is equal to, activated carbon supplementary quantity Q adjusted up, new activated carbon per unit time determines supplementary device makeup flow W Make up .
  8. 根据权利要求3所述的方法，其特征在于，按照下述步骤根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p： The method according to claim 3, wherein the given frequency f g and the discharge of the feeding device in the activated carbon concentration analysis activation subsystem are adjusted according to the operating frequency f c of the belt scale according to the following steps The given frequency f p of the device :
    确定所述皮带秤的下料流量W C＝K c×f c，给料装置的下料流量W G＝K g×f g，排料装置的下料流量W P＝K p×f p；式中，Kc、K g和K p均为常数； Determining the discharge flow rate of the belt weigher W C = K c × f c , the discharge flow rate of the feeding device W G = K g × f g , the discharge flow rate of the discharge device W P = K p × f p ; Where Kc, K g and K p are constants;
    控制所述活性炭集中解析活化子系统的给料装置、排料装置和皮带秤的下料流量相同，使得W G＝W P＝W C＝W X0； The feeding flow rate of the feeding device, the discharging device and the belt weigher for controlling the activated carbon centralized analytical activation subsystem is the same, so that W G = W P = W C = W X0 ;
    根据上式，得到所述给料装置的给定频率f g与皮带秤的运行频率f c之间满足下式关系：
    Figure PCTCN2018083579-appb-100018
    以根据上式及皮带秤的运行频率f c，调整给料装置的给定频率f g；以及，     According to the above formula, the relationship between the given frequency f g of the feeding device and the operating frequency f c of the belt weigher is obtained:
    Figure PCTCN2018083579-appb-100018
    Adjusting the given frequency f g of the feeding device according to the above formula and the operating frequency f c of the belt weigher;
    得到所述排料装置的给定频率f p与皮带秤的运行频率f c之间满足下式关系：
    Figure PCTCN2018083579-appb-100019
    以根据上式及皮带秤的运行频率f c，调整排料装置的给定频率f p。     Obtaining the following relationship between the given frequency f p of the discharge device and the operating frequency f c of the belt scale:
    Figure PCTCN2018083579-appb-100019
    The given frequency f p of the discharge device is adjusted according to the above formula and the operating frequency f c of the belt weigher.
  9. 一种多工序烟气净化系统的控制方法，其特征在于，包括以下步骤：A method for controlling a multi-process flue gas purification system, comprising the steps of:
    确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100020
    以及，确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100021
    其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间；     Determining the activated carbon circulation flow rate of the flue gas purification device in the sintering process corresponding to the current time t
    Figure PCTCN2018083579-appb-100020
    And determining the circulating flow rate of the activated carbon of the flue gas purification device in the process n corresponding to the time t ni
    Figure PCTCN2018083579-appb-100021
    Where n is the serial number of each step in the multi-process flue gas purification system; t ni = tT ni , T ni is the time during which the flue gas purification device corresponding to the flue gas purification device in step n is transported to the activated carbon centralized analytical activation subsystem at time i;
    根据所述工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100022
    和烧结工序中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100023
    以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0；     According to the activated carbon circulation flow rate of the flue gas purification device in the process n
    Figure PCTCN2018083579-appb-100022
    Activated carbon circulation flow rate of the flue gas purification device in the sintering process
    Figure PCTCN2018083579-appb-100023
    And the following formula, determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
    Figure PCTCN2018083579-appb-100024
    Figure PCTCN2018083579-appb-100024
    根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取
    Figure PCTCN2018083579-appb-100025
    时对应的所述皮带秤的运行频率f c；     Adjusting the flow rate W C0 of the belt scale according to the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem; and obtaining
    Figure PCTCN2018083579-appb-100025
    Corresponding operating frequency f c of the belt scale;
    根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 Adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize the multi-process flue gas purification system control.
  10. 根据权利要求9所述的方法，其特征在于，还包括：The method of claim 9 further comprising:
    根据所述烧结工序中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100026
    以及式
    Figure PCTCN2018083579-appb-100027
    确定烧结工序卸料装置的卸料流量W 卸1；其中，j为系数，取值范围为0.9～0.97；以及，控制所述工序n卸料装置的卸料流量W 卸2为最大。     According to the activated carbon circulation flow rate of the flue gas purification device in the sintering process
    Figure PCTCN2018083579-appb-100026
    And
    Figure PCTCN2018083579-appb-100027
    The discharge flow rate W of the unloading device of the sintering process is determined to be 1 ; wherein j is a coefficient, and the value ranges from 0.9 to 0.97; and the discharge flow W of the unloading device of the process n is controlled to be the maximum.
  11. 一种多工序烟气净化系统的控制方法，其特征在于，包括以下步骤：A method for controlling a multi-process flue gas purification system, comprising the steps of:
    确定当前时刻t对应的烧结工序中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100028
    确定t ni时刻对应的工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100029
    以及，确定新活性炭补充装置的补充新活性炭的补充流量W 补；其中，n为多工序烟气净化系统中各工序的序号；t ni＝t-T ni，T ni为工序n中烟气净化装置在i时刻对应的污染活性炭运输至活性炭集中解析活化子系统的时间；     Determining the activated carbon circulation flow rate of the flue gas purification device in the sintering process corresponding to the current time t
    Figure PCTCN2018083579-appb-100028
    Determine the activated carbon circulation flow rate of the flue gas purification device in the process n corresponding to the time t ni
    Figure PCTCN2018083579-appb-100029
    And determining to add new makeup flow W complement activated carbon GAC replenishing apparatus; wherein, n is a multi-step gas purification system number of each step; t ni = tT ni, T ni n is a step in the flue gas purifying device The time at which the contaminated activated carbon corresponding to the time i is transported to the activated carbon to resolve the activation subsystem;
    根据所述工序n中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100030
    烧结工序中烟气净化装置的活性炭循环流量
    Figure PCTCN2018083579-appb-100031
    和补充流量W 补，以及下式，确定当前时刻t对应的活性炭集中解析活化子系统的活性炭循环流量W X0；     According to the activated carbon circulation flow rate of the flue gas purification device in the process n
    Figure PCTCN2018083579-appb-100030
    Activated carbon circulation flow rate of flue gas purification device in sintering process
    Figure PCTCN2018083579-appb-100031
    And the supplementary flow W supplement , and the following formula, determining the activated carbon circulating flow W X0 of the activated carbon centralized analytical activation subsystem corresponding to the current time t;
    Figure PCTCN2018083579-appb-100032
    Figure PCTCN2018083579-appb-100032
    根据所述活性炭集中解析活化子系统的活性炭循环流量W X0，调整皮带秤的下料流量W C；以及，获取
    Figure PCTCN2018083579-appb-100033
    时对应的所述皮带秤的运行频率f c；     Adjusting the flow rate W C0 of the belt scale according to the activated carbon circulating flow W X0 of the activated carbon concentration analysis activation subsystem; and obtaining
    Figure PCTCN2018083579-appb-100033
    Corresponding operating frequency f c of the belt scale;
    根据所述皮带秤的运行频率f c，调整所述活性炭集中解析活化子系统中 给料装置的给定频率f g和排料装置的给定频率f p，以实现对多工序烟气净化系统的控制。 Adjusting a given frequency f g of the feeding device in the activated carbon concentration analysis activation subsystem and a given frequency f p of the discharging device according to the operating frequency f c of the belt scale to realize the multi-process flue gas purification system control.
PCT/CN2018/083579 2018-01-29 2018-04-18 Multi-process flue gas purification system and method for controlling same WO2019144523A1 (en)

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