KR102318293B1 - Multi-process flue gas purification system and its control method - Google Patents

Abstract

The present invention discloses a multi-process flue gas purification system and a control method therefor, wherein the centralized desorption subsystem and the sintering process subsystem are installed in a sintering process to form an integrated structure with the adsorption subsystem of the sintering process. It allows the activated carbon circulating between them to complete the cycle through the transport device group, and does not require additional transport equipment, thereby saving transport resources and at the same time weakening the impact on the system operation during transport. In the present invention, the concentrated desorption subsystem includes a material distribution device, and distributes the activated carbon to the adsorption subsystem of the sintering process through the first material distribution member, the activated carbon flow rate of the concentrated desorption subsystem, the adsorption subsystem of the sintering process, and the remaining adsorption The equilibrium relationship between the concentrated desorption subsystem and the adsorption subsystem on the side of the concentrated desorption subsystem by making the activated carbon flow rates of the subsystems equalize with each other and setting the operating parameters of the material intake device, the material discharge device and the material distribution device of the concentrated desorption subsystem to achieve precise control over

Description

Multi-process flue gas purification system and its control method

The present invention relates to the field of gas purification technology, and more particularly, to a flue gas purification system involving a multi-process and a method for controlling the same.

There are numerous processes within the steel industry that can emit flue gases, such as sintering processes, coking processes, blast furnace ironmaking processes, rotary or electric furnace steelmaking processes, etc. The flue gas emitted from each process contains a large amount of dust, contaminants such as _{SO 2} and NO _X. In general, enterprises use activated carbon flue gas purification technology _{to remove SO 2} and NO _X in flue gas to realize clean emission of enterprise waste.

1 shows an activated carbon flue gas purification system, comprising an adsorption subsystem 100 for purifying raw (untreated) flue gas and discharging contaminated activated carbon, desorption for activating contaminated activated carbon and discharging activated activated carbon It includes a subsystem 200, an antacid (acid production) subsystem (not shown) for recycling the _{pollutants SO 2} and NO _{X, and two activated carbon transporters 310 and 320 .} Here, the adsorption subsystem 100 includes an adsorption tower 101 , a material introduction device 102 , and a material discharge device 103 , and the desorption subsystem 200 includes a desorption activation tower 201 , a material introduction device 202 and and a material discharging device 203 . When the system is operated, the activated carbon transported by the transport device 310 is introduced into the adsorption tower 101 through the material introduction device 102 to form an activated carbon material layer in the adsorption tower 101 and simultaneously remove contaminants SO ₂ and NO _X The contained original flue gas is constantly introduced into the adsorption tower 101 and further flows into the activated carbon material layer so that SO ₂ and NO _X in the original flue gas are adsorbed by the activated carbon, so that it is discharged as clean flue gas. . The material discharging device 103 of the adsorption subsystem 100 continuously operates _{to discharge the contaminated activated carbon in which SO 2} and NO _X are collected in a large amount in the adsorption tower 101 , and then the desorption sub-system by the conveying device 320 . Transport to 200. The contaminated activated carbon transported by the transport device 320 is introduced into the desorption activation tower 201 through the material introduction device 202 _{so that contaminants such as SO 2} and NO _X are desorbed from the contaminated activated carbon to become activated activated carbon. The material discharging device 203 discharges the activated activated carbon of the desorption activation tower 201 and is transported to the adsorption subsystem 100 by the conveying device 310 to be recycled.

One application of the activated carbon flue gas purification system shown in Fig. 1 is that an enterprise installs a set of adsorption subsystems and a set of desorption subsystems in each flue gas discharge process, and each set of adsorption subsystems and The desorption subsystem works simultaneously to complete the purification of polluted flue gas from each process of the enterprise. However, the drawback of this application is that the number of detachable subsystems is too large. Injecting a large amount of the detachable subsystem not only wastes equipment resources, but also increases the management difficulty of the company. In a second application to this deficiency, an enterprise installs only one set of adsorption subsystems for each flue-gassing process, and then installs at least one concentrated desorption subsystem exclusively for the intensive treatment of contaminated activated carbon for the entire plant. Corresponding to some or all of the adsorption subsystems within the range allows for a one-to-many correspondence between the concentrated desorption subsystem and the adsorption subsystem.

In the second application mode, firstly, the original flue gas flow rate entering the adsorption subsystem, the contaminant content in the original flue gas and the circulating flow rate of activated carbon in the adsorption subsystem are major factors affecting the flue gas purification effect, For example, when the original flue gas flow rate increases and/or the contaminant content in the flue gas increases, the circulating flow rate of activated carbon in the adsorption subsystem must also be quantitatively increased at the same time to ensure the flue gas purification effect, otherwise Activated carbon is already saturated and some contaminants in the original flue gas are not adsorbed, which may reduce the purification effect. Therefore, how to balance the relationship between elements such as the circulation flow rate of the activated carbon in the adsorption subsystem and the original flue gas flow rate has become a technical challenge that is difficult for those of ordinary skill in the art to overcome.

Next, the concentrated desorption subsystem intensively performs activation treatment on the contaminated activated carbon discharged from a plurality of adsorption subsystems. In addition, the contaminated activated carbon treated by the centralized desorption subsystem is derived from the adsorption subsystem installed in a different process, and the stability of the amount of activated carbon emitted by the adsorption subsystem of the different process is also affected due to factors such as equipment failure and production plan adjustment. , how to control the equilibrium of the treatment capacity of the concentrated desorption subsystem for the contaminated activated carbon and the activated carbon emission of the multiple adsorption subsystems is a technical difficulty that is difficult for those of ordinary skill in the art to overcome. became

The present invention provides a multi-process flue gas purification system and a control method therefor. A technical problem of how to accurately control the equilibrium between a concentrated desorption subsystem and a plurality of adsorption subsystems corresponding thereto under the premise of ensuring the flue gas purification effect can solve

In a first aspect, the present invention provides a multi-process flue gas purification system, wherein the purification system includes a plurality of adsorption subsystems respectively installed in each flue gas discharge process, a concentrated desorption subsystem corresponding to the plurality of adsorption subsystems, and a transport sub-system. a system, wherein the adsorption subsystem comprises an adsorption tower, a feeding apparatus for transporting activated activated carbon to the adsorption tower, and a discharging apparatus for discharging contaminated activated carbon in the adsorption tower; the concentrated desorption subsystem includes a desorption activation tower, a material intake device for transporting contaminated activated carbon to the desorption activation tower, and a material discharge device for discharging the activated activated carbon in the desorption activation tower;

the centralized desorption subsystem is installed in the sintering process;

The centralized desorption subsystem,

A material distributing apparatus comprising at least a first material distributing member for distributing the activated carbon to an adsorption subsystem of a sintering process and a second material distributing member for distributing the remaining activated carbon to an adsorption subsystem of another process ;

The contaminated activated carbon discharged by the adsorption subsystem of the sintering process is transported to the top buffer warehouse of the centralized desorption subsystem, and the activated activated carbon distributed by the first material distribution member is transported to the top buffer warehouse of the adsorption subsystem of the sintering process. It further includes a carrier group for

In a first possible embodiment of the first aspect in conjunction with the first aspect, the centralized desorption subsystem comprises:

a contaminated activated carbon warehouse for storing the contaminated activated carbon discharged by the adsorption subsystem; and a first unloading device for unloading the contaminated activated carbon in the contaminated activated carbon warehouse to the conveying device below the tower.

In conjunction with the first aspect or a first possible embodiment of the first aspect, the centralized desorption subsystem comprises:

a vibrating body (sieve) installed under the material discharging device of the desorption subsystem to separate the spent activated carbon in the activated activated carbon;

Further comprising; a new additional activated carbon warehouse and a second unloading device installed above the contaminated activated carbon warehouse, wherein the second unloading device is for unloading the activated carbon in the new additional activated carbon warehouse to the contaminated activated carbon warehouse.

In a second aspect, the present invention provides a method for controlling a multi-process flue gas purification system, wherein the multi-process flue gas purification system is the flue gas purification system described in the first aspect of the present invention, the method comprising the steps of do.

determining a real-time flow rate of activated carbon in an adsorption subsystem corresponding to the concentrated desorption subsystem;

Determine the theoretical equilibrium flow rate of the activated carbon at the current time of the concentrated desorption subsystem based on the flow rate of the activated carbon at the time _{t i} of each adsorption subsystem _{, wherein the time difference between the time t i} and the current time causes the contaminated activated carbon to be concentrated from each adsorption subsystem the time required to cycle to the desorption subsystem;

Based on the theoretical equilibrium flow rate of the activated carbon at the current time of the centralized desorption subsystem, the operating parameters of the material intake device and the material discharge device of the centralized desorption subsystem are set, and the activated carbon flow rate at the time _{t i of the absorption subsystem of the sintering process is set.} realizing control over the flue gas purification system by setting operating parameters of the first material distribution member and the second material distribution member according to the method.

Using the embodiment of the present invention for the multi-process flue gas purification system, the centralized desorption subsystem and the sintering process sub-system are installed in the sintering process to form an integral structure with the adsorption subsystem of the sintering process. Activated carbon circulating between systems can complete circulation through a transport group without additional transport equipment, saving transport resources and reducing the impact on system operation during transport. In an embodiment of the present invention, the activated carbon is distributed to the adsorption subsystem of the sintering process through the first material distribution member by installing a material distribution device in the centralized desorption subsystem, and the activated carbon flow rate of the desorption subsystem is set in the adsorption subsystem of the sintering process and between the concentrated desorption subsystem and the adsorption subsystem on the side of the concentrated desorption subsystem by setting the operating parameters of the material intake device, the material discharge device and the material distribution device of the concentrated desorption subsystem to be balanced with the activated carbon flow rate of other adsorption subsystems Accurate control of the equilibrium relationship of

In a first possible embodiment of the second aspect in conjunction with the second aspect, a real-time flow rate of activated carbon in the adsorption subsystem corresponding to the concentrated desorption subsystem is determined according to the following steps.

obtaining an original flue gas flow rate entering the adsorption subsystem and a contaminant content in the flue gas;

obtaining a flow rate of a pollutant in the original flue gas based on the original flue gas flow rate and a pollutant content in the flue gas;

determining a theoretical flow rate of the activated carbon of the adsorption subsystem based on the flow rate of the contaminants in the original flue gas, and determining the theoretical flow rate of the activated carbon of the adsorption subsystem as a real-time flow rate.

Since the original flue gas flow rate and the contaminant content in the flue gas change from moment to moment, this embodiment is based on the original flue gas flow rate entering each adsorption subsystem and the contaminant content in the flue gas, the real-time flow rate of activated carbon in each adsorption subsystem By determining this, it is possible to ensure the flue gas purification effect and to save activated carbon resources at the same time.

In conjunction with the first possible embodiment of the second aspect, in a second possible embodiment of the second aspect, based on the original flue gas flow rate and the pollutant content in the flue gas, the flow rate of pollutants in the original flue gas according to the following equation calculate,

는 각 흡착 서브 시스템에 진입하는 원래의 연도가스 중의 오염물 SO₂의 유량, kg/h이고; here

_{is the flow rate of contaminant SO 2} in the original flue gas entering each adsorption subsystem, kg/h;

는 흡착 서브 시스템에 진입하는 원래의 연도가스 중의 오염물 SO₂의 함량, mg/Nm³이며;

_{is the content of contaminant SO 2} in the original flue gas entering the adsorption subsystem, mg/Nm ³ ;

는 흡착 서브 시스템에 진입하는 원래의 연도가스 중의 오염물 NO_X의 유량, kg/h이고;

_{is the flow rate of pollutant NO X} in the original flue gas entering the adsorption subsystem, kg/h;

는 흡착 서브 시스템에 진입하는 원래의 연도가스 중의 오염물 NO_X의 함량, mg/Nm³이며;

_{is the content of pollutant NO X} in the original flue gas entering the adsorption subsystem, mg/Nm ³ ;

는 흡착 서브 시스템에 진입하는 원래의 연도가스 유량, Nm³/h이고;

is the original flue gas flow rate entering the adsorption subsystem, Nm ³ /h;

i is the sequence number of the process in which the adsorption subsystem is located;

Determine the theoretical flow rate of activated carbon in the adsorption subsystem according to the following equation based on the flow rate of contaminants in the original flue gas,

는 흡착 서브 시스템의 활성탄의 이론적 유량, kg/h이고; here

is the theoretical flow rate of activated carbon in the adsorption subsystem, kg/h;

K ₁ is a constant and generally takes 15-21; K ₂ is a constant and generally takes 3-4.

By using this embodiment, the real-time flow rate of activated carbon of each adsorption subsystem is accurately and quantitatively calculated based on the original flue gas flow rate and the contaminant content in the flue gas, so that the data is used for accurate control of the flue gas purification system of the present invention. will provide

_{In conjunction with the second possible embodiment of the second aspect, based on the activated carbon flow rate at time t i} of the adsorption subsystem in a third possible embodiment of the second aspect, the theoretical current time activated carbon of the concentrated desorption subsystem according to the following equation Determine the equilibrium flow,

Q _{X0 current} ΣQ = _{Xi (ti)}

Q _X1(ti) =Q _X1Current

where Q _X0current is the current visual theoretical equilibrium flow rate of activated carbon in the concentrated desorption subsystem, kg/h;

는 집중 탈착 서브 시스템과 대응되는 흡착 서브 시스템의 t_i시각에서의 활성탄 유량, kg/h이며;

is the activated carbon flow rate, kg/h, at time _{t i} of the concentrated desorption subsystem and the corresponding adsorption subsystem;

는 소결 공정의 흡착 서브 시스템의 t_i시각에서의 활성탄 유량, kg/h이고;

is the activated carbon flow rate, kg/h, at time _{t i} of the adsorption subsystem of the sintering process;

Q _{X1 present} is the current hourly circulating flow rate of activated carbon in the adsorption subsystem of the sintering process, kg/h.

In this embodiment, the time required for the contaminated activated carbon to circulate from each adsorption subsystem to the concentrated desorption subsystem is cleverly used _{to determine the ti} time corresponding to the current time of each adsorption subsystem, and Accurately determine the theoretical equilibrium flow rate of activated carbon at the current time of the concentrated desorption subsystem based on the activated carbon flow rate at time t _i , wherein the concentrated desorption subsystem is installed in the sintering process and the contaminated activated carbon is transferred from the adsorption subsystem of the sintering process to the concentrated desorption sub-system Since the time required to cycle to the system is 0, the time t1 and the current time are the same.

In conjunction with the second possible embodiment of the second aspect, in a fourth possible embodiment of the second aspect, based on the theoretical equilibrium flow rate of the current visual activated carbon of the centralized desorption subsystem, the mass intake device and the material discharge device of the centralized desorption subsystem according to the following steps Set the operating parameters of the device.

determining the theoretical flow rates of the material intake device and the material discharge device of the concentrated desorption subsystem based on the current visual theoretical equilibrium flow rate of the activated carbon of the concentrated desorption subsystem;

determining a theoretical operating frequency of the material intake device and the material discharge device based on the theoretical flow rates of the material intake device and the material discharge device;

setting a given frequency of the material withdrawing device and the material ejecting device based on the theoretical operating frequencies of the material taking-in device and the material-discharging device.

The present embodiment realizes and operates an accurate control over the equilibrium relationship between the concentrated desorption subsystem and the adsorption subsystem on the centralized desorption subsystem side by setting a given frequency of the substance intake device and the substance exhaust device of the centralized desorption subsystem This is simple, easy to implement and highly reliable.

In conjunction with the fourth possible embodiment of the second aspect, a fifth possible embodiment of the second aspect determines the theoretical flow rates of the mass intake device and the mass discharge device of the centralized desorption subsystem according to the formula:

Q ₀ = Q _{0 binary times = Q X0 (t) × j} ;

where Q ₀ is the theoretical flow rate of the mass intake device of the desorption subsystem, kg/h;

Q _{0 times} is the theoretical flow rate of the mass ejection device of the desorption subsystem, kg/h;

j is a constant, usually 0.9 to 0.97;

Determining the theoretical operating frequency of the material intake device and the material discharge device according to the following equation,

f _binary =Q _binary /K _binary

f _times =Q _{times 0} /K _times

Where f is theoretically _true operating frequency of the material inlet of the concentration unit and the detachable subsystem;

f _times the theoretical operating frequency of the material discharge apparatus of the focus subsystem and desorption;

K _true and K _times are constants, and the unit is kg/(h Hz).

Using the present embodiment, it is possible to accurately calculate the theoretical operating frequency based on the theoretical flow rate and based on the quantitative relationship between the theoretical operating frequency and the theoretical flow rate of the material taking-in device and the material-discharging device, and the given operation of the material feeding device and the material discharging device By adjusting the frequency to this theoretical operating frequency, the purpose of controlling the mass inlet flow rate and the mass outlet flow rate of the centralized desorption subsystem can be reached, so that accurate control of the flue gas purification system can be realized.

In conjunction with the fifth possible embodiment of the second aspect, a sixth possible embodiment of the second aspect is based on the activated carbon flow rate at time _{t i of the adsorption subsystem of the sintering process, comprising the steps of:}

determining a material dispensing flow rate of the first material dispensing member based on the equation Q _min1(t) =Q _X1(t)×j;

determining a theoretical operating frequency of the first material dispensing member based on the material dispensing flow rate of the first material dispensing member;

setting a given frequency of the first material dispensing member based on the theoretical operating frequency of the first material dispensing member; and

setting the operating parameters of the first material dispensing member and the second material dispensing member according to; setting a given frequency of the second material dispensing member to a maximum;

where Q _{min 1(t)} is the mass distribution flow rate of the first material distribution member, kg/h.

Using this embodiment, a given frequency is determined according to the theoretical operating frequency based on the quantitative relationship between the theoretical operating frequency of the first material dispensing member and its material dispensing flow rate, and the given frequency of the first material dispensing member is set as this theoretical operating frequency. By controlling the sintering process and the corresponding adsorption subsystem, the purpose of controlling the flow rate of the activated carbon is reached, and at the same time, by maximally adjusting the given frequency of the second material distribution member, the calculation and control steps are simplified and the stable operation of the flue gas purification system is achieved. ensure the operation

In a seventh possible embodiment of the second aspect in conjunction with the second aspect, the method comprises:

and realizing accurate control for each adsorption subsystem by setting the operating parameters of the material intake device and the material discharge device of the absorption subsystem according to the theoretical flow rate of the activated carbon in the absorption subsystem.

In a third aspect an embodiment of the present invention provides a method for controlling a multi-process flue gas purification system, wherein the multi-process flue gas purification system is the flue gas purification system described in the first possible embodiment of the first aspect of the present invention and said method silver,

determining a real-time flow rate of activated carbon in an adsorption subsystem corresponding to the concentrated desorption subsystem;

Determine the theoretical equilibrium flow rate of the activated carbon at the current time of the concentrated desorption subsystem based on the flow rate of the activated carbon at the time _{t i} of each adsorption subsystem _{, wherein the time difference between the time t i} and the current time causes the contaminated activated carbon to be concentrated from each adsorption subsystem the time required to cycle to the desorption subsystem;

setting operation parameters of a material intake device and a material discharge device of the concentrated desorption subsystem based on the current visual theoretical equilibrium flow rate of activated carbon of the concentrated desorption subsystem;

setting operating parameters of the first material distribution member and the second material distribution member based on the activated carbon flow rate at time _{t i} of the adsorption subsystem of the sintering process; and

Control for the focus desorption sub-above with the theoretical equilibrium of the current time the activated carbon of the system flow rate and the adsorption subsystem of the sintering process based on the activated carbon flow rate in t _i the time by setting the operating parameter of the first unloading device the flue gas purification system including the step of realizing

In a fourth aspect an embodiment of the present invention provides a method for controlling a multi-process flue gas purification system, wherein the multi-process flue gas purification system is the flue gas purification system described in the second possible embodiment of the first aspect of the present invention and the method silver,

determining a real-time flow rate of activated carbon of the intensive desorption subsystem and the corresponding adsorption subsystem;

Determine the theoretical equilibrium flow rate of the activated carbon at the current time of the concentrated desorption subsystem based on the flow rate of the activated carbon at the time _{t i} of each adsorption subsystem _{, wherein the time difference between the time t i} and the current time causes the contaminated activated carbon to be concentrated from each adsorption subsystem the time required to cycle to the desorption subsystem;

setting operation parameters of a material intake device and a material discharge device of the concentrated desorption subsystem based on the current visual theoretical equilibrium flow rate of activated carbon of the concentrated desorption subsystem;

setting operating parameters of the first material distribution member and the second material distribution member based on the activated carbon flow rate at time _{t i} of the adsorption subsystem of the sintering process; and

and realizing control of the flue gas purification system by setting operating parameters of the second unloading device based on the consumed activated carbon flow rate selected by the vibrating body.

As can be seen from the above technical solution, the multi-process flue gas purification system and control method of the present invention provide a concentrated desorption sub-system by installing a concentrated desorption subsystem in the sintering process to form an integrated structure with the adsorption subsystem of the sintering process. The activated carbon circulating between the system and the adsorption subsystem of the sintering process can complete the circulation through the transport device group, so there is no need for additional transport equipment, thereby saving transport resources and reducing the impact on system operation during transport. Reduce. By installing a material distribution device in the centralized desorption subsystem, the activated carbon is distributed to the adsorption subsystem of the sintering process through the first material distribution member, and the activated carbon flow rate of the concentrated desorption subsystem and the adsorption subsystem of the sintering process and other adsorption subsystems are By ensuring the activated carbon flow rates are balanced with each other, and setting the operating parameters of the mass intake device, the material discharge device and the mass distribution device of the concentrated desorption subsystem, the accurate analysis of the equilibrium relationship between the concentrated desorption subsystem and the adsorption subsystem on the side of the concentrated desorption subsystem Realize control.

In order to more clearly explain the technical solution of the present invention, drawings to be used in the following embodiments are briefly introduced, based on these drawings on the premise that creative efforts are not made to those of ordinary skill in the art to which the present invention pertains. It is obvious that other drawings may be obtained.
1 is a structural schematic diagram of a prior art activated carbon flue gas purification system;
2 is a structural schematic diagram of a multi-process flue gas purification system of the prior art;
3 is a structural schematic diagram of a multi-process flue gas purification system shown in an embodiment of the present invention;
Fig. 4 is a flow chart of a control method of a multi-process flue gas purification system according to an exemplary embodiment of the present invention;
5 is a flow chart of a control method of a multi-process flue gas purification system according to a preferred embodiment of the present invention;
6 is a flowchart of a control method of a multi-process flue gas purification system according to another preferred embodiment of the present invention;
7 is a flowchart of a control method of a multi-process flue gas purification system according to another preferred embodiment of the present invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, exemplary embodiments will be described in detail and examples thereof will be shown in the drawings. When the following description relates to drawings, the same numbers in different drawings refer to the same or similar elements, unless otherwise indicated. The embodiments described in the illustrative examples below are not representative of all embodiments consistent with the present invention. To the contrary, these are merely examples of devices and methods consistent with some aspects of the invention as set forth in the appended claims.

2 shows a multi-process flue gas purification system. Referring to FIG. 2, the flue gas purification system comprises:

A plurality of adsorption subsystems (110/120/130, etc.) respectively installed in each flue gas discharge process, a concentrated desorption subsystem 200 corresponding to the plurality of adsorption subsystems, and a transport subsystem (not shown) are included. , the polluted activated carbon emitted by each adsorption subsystem is transported to the centralized desorption subsystem through the transport subsystem for intensive activation treatment, and in one set of flue gas purification systems, the concentrated desorption subsystem and each adsorption subsystem are form a multi-relationship.

Here, the concentrated desorption subsystem 200 includes a desorption activation tower 201 , a material introduction device 202 for introducing contaminated activated carbon into the desorption activation tower 201 , and a desorption activation tower 201 for discharging the activated activated carbon from the desorption activation tower 201 . a material discharging device (203), comprising a conveying device (204) for transporting the contaminated activated carbon from below the tower to the top of the tower; Taking the adsorption subsystem 110 as an example, in the present invention, each of the adsorption subsystems includes an adsorption tower 111, a material introduction device 112 for introducing activated activated carbon into the adsorption tower 111, and an adsorption tower for contaminated activated carbon ( 111), a material discharging device 113 for discharging from the tower, a conveying device 114 for transporting the activated activated carbon from below the tower to the top of the tower, and an activated activated carbon warehouse 115 for storing the activated activated carbon and its unloading device 116 .

When the system is in operation, activated activated carbon (which may include new additional activated carbon) is continuously fed into the buffer warehouse 117 from the side of the adsorption subsystem, and then enters the adsorption tower 111 through the material introduction device 112 and enters the adsorption tower 111 ), the activated carbon adsorbs contaminants in the original flue gas and moves from top to bottom at the same time, and is finally discharged from the adsorption tower 111 from the material discharging device 113 . The contaminated activated carbon discharged from the adsorption subsystem is transported to the centralized desorption subsystem 200 through the transport subsystem, where the contaminated activated carbon is transported by a specialized transport vehicle in some adsorption subsystems that are far from the centralized desorption subsystem do.

On the side of the centralized desorption subsystem 200, the contaminated activated carbon from multiple adsorption subsystems is transported from the bottom of the tower to the buffer warehouse at the top of the desorption tower by a conveying device 204, and the contaminated activated carbon is transported through the material intake device 202. It enters the desorption activation tower 201 to proceed with activation. After reaching the bottom, it is discharged by the material discharge device 203, and the activated activated carbon is transported back to the adsorption subsystem of each process by the transport subsystem and recycled.

On the basis of the system shown in FIG. 2, the present invention provides a multi-process flue gas purification system. As shown in FIG. 3, in the multi-process flue gas purification system provided by the present invention, the concentrated desorption subsystem 200 is installed in the sintering process;

The centralized desorption subsystem 200,

at least a first material distribution member 2121 for distributing the activated activated carbon to the adsorption subsystem 110 of the sintering process and a second material distribution member 2122 for distributing the remaining activated carbon to the adsorption subsystem of the other process; a material dispensing device 212 to;

The contaminated activated carbon discharged by the adsorption subsystem 110 of the sintering process is transported to the buffer warehouse at the top of the tower of the centralized desorption subsystem 200, and the activated activated carbon distributed by the first material distribution member 2121 is adsorbed in the sintering process It further includes a group of transporters for transporting to the buffer warehouse atop the tower of the subsystem.

As shown in FIG. 3 , the transport device group includes a first transport device 210 and a second transport device 211 .

Based on the actual situation of production of steel enterprises, the amount of flue gas generated in the sintering process is 70% of the total amount of flue gas of the enterprise, which means that the amount of activated carbon required by the adsorption subsystem of the sintering process is relatively large. Based on this, a centralized desorption subsystem is installed in the sintering process so that the centralized desorption subsystem forms an integral structure with the adsorption subsystem of the sintering process, so that the activated carbon circulating between the centralized desorption subsystem and the sintering process subsystem is transported Through the device group, the cycle can be completed, and there is no need for additional transport equipment, thereby saving transport resources and reducing the impact on the system operation of the transport process.

After the centralized desorption subsystem is installed in the sintering process, a large amount of original flue gas generated in the sintering process enters the adsorption subsystem 110 of the sintering process through a conduit, and contaminated activated carbon generated in the adsorption subsystem 110 of the sintering process Silver is directly transported to the centralized desorption subsystem 200 through the transport device 210 , and activated carbon generated in the centralized desorption subsystem is transported directly to the adsorption subsystem 110 of the sintering process by the transport device 211 .

In addition, a first material distribution member 2121 and a second material distribution member 2122 are included to install the material distribution device 212 in the centralized desorption subsystem. The activated activated carbon required for the adsorption subsystem 110 of the sintering process is pre-distributed through the first material distribution member 2121 , and directly unloaded into the transport device 211 , and the adsorption subsystem of the sintering process by the transport device 211 . It is transported and loaded directly on top of the system, which corresponds to internal circulation. At the same time, the activated activated carbon unloaded by the second material distribution member 2122 is respectively transported to the adsorption subsystem of the remaining process by the transport subsystem, which corresponds to an external circulation.

In some preferred embodiments, the centralized desorption subsystem 200,

a contaminated activated carbon storage 205 for storing the contaminated activated carbon discharged by the adsorption subsystem; and a first unloading device 206 for unloading the contaminated activated carbon from the contaminated activated carbon warehouse to the second conveying device 211 .

In some other preferred embodiments, the centralized desorption subsystem 200 is,

a vibrating body 209 installed under the material discharging device 203 of the concentrated desorption subsystem 200 to separate the spent activated carbon in the activated activated carbon;

Further comprising a new additional activated carbon warehouse 207 and a second unloading device 208 installed on the contaminated activated carbon warehouse 205, the second unloading device 208 is a newly added activated carbon warehouse (207) For unloading the activated carbon to the contaminated activated carbon warehouse (205).

It should be explained that the new additional activated carbon is for supplementing the consumption generated in the process of circulating or adsorbing the activated carbon, and for adjusting the activated carbon circulation flow rate of the centralized desorption subsystem.

When the flue gas purification system shown in FIG. 3 of the present invention is operated, the contaminated activated carbon from a plurality of adsorption subsystems on the centralized desorption subsystem 200 is temporarily stored in the contaminated activated carbon warehouse 205 and then is first unloaded. By unloading the contaminated activated carbon from the warehouse at a constant flow rate through the device 206 to the transport device 210, and simultaneously unloading the contaminated activated carbon discharged by the adsorption subsystem 110 of the sintering process to the transport device 210, The transport device 210 uniformly transports the desorption tower from the bottom of the tower to the buffer warehouse at the top of the desorption tower, and the contaminated activated carbon is introduced into the desorption activation tower 201 through the material introduction device 202 to proceed with activation, and the material after reaching the bottom After being discharged by the discharging device 203, the activated activated carbon may be transported back to the adsorption subsystem of each process by the transport subsystem and recycled. In the actual operation of the system, consumption of activated carbon is inevitable. In the present invention, too fine spent activated carbon is discharged through the vibrating body 209 and new activated carbon can be added to the system at the same time.

In the present invention, activated carbon is circulated between the adsorption subsystem and the centralized desorption subsystem to allow the flue gas purification system to form a plurality of closed circulation structures. The system 110 forms one closed circulation structure, and the concentrated desorption subsystem forms a closed circulation structure different from the adsorption subsystem of the coking process.

Based on this circulation structure, the applicant found that the continuous, stable and effective operation of the flue gas purification system can be ensured only when the sum of the activated carbon flow rates of each adsorption subsystem is theoretically equal to the activated carbon flow rate of the concentrated desorption subsystems. did. Using this equivalence relationship, the present invention provides a control method for the multi-process flue gas purification system, in which the equilibrium between the concentrated desorption subsystem and a plurality of corresponding adsorption subsystems is accurately achieved on the premise of ensuring the flue gas purification effect. It solves the technical problem of whether to control.

4 is a flowchart of a control method of a multi-process flue gas purification system shown according to an exemplary embodiment of the present invention. It should be noted that the method of the present invention is installed in a computer and the performance is controlled by the computer. Referring to FIG. 4 , the method includes the following steps.

Step 110, determining the real-time flow rate of the activated carbon of the adsorption subsystem corresponding to the concentrated desorption subsystem;

In the present invention, a set of flue gas purification systems includes several adsorption subsystems and one centralized desorption subsystem, each adsorption subsystem having a different flue gas discharge process, e.g. sintering, pelletizing, coking It is installed in processes such as furnace, blast furnace ironmaking, rotary or electric furnace steelmaking, rolling, lime kiln, and power plant. Since there are many flue gas emission processes, the present invention distinguishes adsorption subsystems installed in different processes through letter i, where i represents the sequence number of each process. For example, in the present invention, i=1 in the case of the sequence number of the sintering process.

As can be seen from the operation process of the flue gas purification system, the original flue gas flow rate entering the adsorption subsystem, the content of contaminants in the original flue gas, and the activated carbon flow rate of the adsorption subsystem affect the flue gas purification effect. is a major factor. For example, if the flow rate of the original flue gas increases and/or the content of pollutants in the flue gas increases, the flow rate of the activated carbon in the adsorption subsystem must also be increased quantitatively at the same time to ensure the effect of cleaning the flue gas, otherwise the activated carbon Since this is already saturated, some contaminants in the original flue gas are not adsorbed, and thus the purification effect may be reduced.

In other words, the activated carbon flow rate of each adsorption subsystem is not fixed, but changes according to the original flue gas flow rate and the contaminant content in the original flue gas. The activated carbon flow rate is adjusted for each cycle, and other times are not adjusted. In step 110, the change in flow rate is monitored by determining the real-time flow rate at different times of the activated carbon of the adsorption subsystem. For example, the real-time flow rate at 12:00 on January 1, 2018 of the adsorption subsystem of the sintering process is Q _{X1 (01011200)} . where Q _X1 represents the activated carbon flow rate of the adsorption subsystem.

It should be further explained that the present invention may choose to adjust the activated carbon flow rate of the adsorption subsystem through a mass intake device or a mass discharge device of the adsorption subsystem.

_{Step 120, based on the activated carbon flow rate at time t i} of each adsorption subsystem, determine the theoretical equilibrium flow rate of the activated carbon at the current time of the concentrated desorption subsystem, wherein _{the time difference between the time t i} and the current time is that the contaminated activated carbon is each adsorbed is the time required to cycle from the subsystem to the concentrated desorption subsystem;

In the actual application of the multi-process flue gas purification system, the location of each flue gas discharge process is different, so that the distance between each adsorption subsystem and the centralized desorption subsystem is also different. This means that the time required for the contaminated activated carbon generated in each adsorption subsystem to circulate to the intensive desorption subsystem is also different. For convenience of explanation, the present invention uses Ti to represent the time required for the contaminated activated carbon to cycle from each adsorption subsystem to the concentrated desorption subsystem. The time required to cycle is T1, the time required for the contaminated activated carbon to cycle from the adsorption subsystem of the coking process to the concentrated desorption subsystem is T2, and so on.

Step 120 of the present invention, based on activated carbon flow rate of each of the adsorption subsystem determine the activated carbon flow rate of the concentrated desorption subsystem, and concentrated desorption subsystems of the activated carbon flow rate in t _i time of each adsorption subsystem corresponding to the concentration desorption Let the current visual and theoretical equilibrium flow rates of activated carbon in the subsystems equilibrate with each other. Contaminated activated carbon is activated carbon in the t _i the time of concentration desorption sub required is a certain amount of time to cycle through the system and the different adsorption subsystems of the corresponding Ti, so the difference of the present invention step 120 includes each of the adsorption subsystem from the respective adsorption subsystem Determine the theoretical equilibrium flow rate of the activated carbon at a current time of the concentrated desorption subsystem according to the flow rate, wherein _{the time difference between the time t i} and the current time is a time required for the contaminated activated carbon to circulate from each adsorption subsystem to the concentrated desorption subsystem, that is, Ti =t _Currently -t _i .

Step 130, based on the theoretical equilibrium flow rate of the activated carbon at the current time of the centralized desorption subsystem, set the operating parameters of the material intake device and the material discharge device of the centralized desorption subsystem, and the activated carbon at the time _{t i of the absorption subsystem of the sintering process} A control for the flue gas purification system is realized by setting operating parameters of the first material distribution member and the second material distribution member according to the flow rate.

In step 130, the operating parameters of the material intake device and the material discharge device of the centralized desorption subsystem are set so that the current instantaneous actual flow rate of activated carbon in the centralized desorption subsystem reaches the theoretical equilibrium flow rate determined in the step 120, so that the concentrated desorption _{The sum of the activated carbon flow rates at time t i} of each adsorption subsystem corresponding to the subsystem and the theoretical equilibrium flow rate of the activated carbon at the current time of the concentrated desorption subsystem are balanced with each other, so that the concentrated desorption subsystem and the adsorption sub-system on the side of the concentrated desorption subsystem Accurately control the equilibrium relationship between the systems.

In addition, by setting an operating parameter of the first material distribution member, the activated carbon flow rate of the first material distribution member and the activated carbon flow rate of the adsorption subsystem of the sintering process are balanced with each other; By setting the operating parameters of the second material distribution member, the activated carbon flow rate of the second material distribution member and the activated carbon flow rate of other adsorption subsystems other than the absorption subsystem of the sintering process are balanced with each other.

As can be seen from the technical conception of the present invention, the step 110 is a key step in realizing the present invention, and the step provides an accurate data basis for the subsequent control process. Actually, there are various embodiments of the step 110, and the present invention provides one preferred embodiment based on the specificity of the application environment. Referring to FIG. 5 , in this preferred embodiment, the real-time flow rate of activated carbon of each adsorption subsystem corresponding to the concentrated desorption subsystem is determined according to the following steps.

Step 210, acquiring the original flue gas flow rate and the contaminant content in the flue gas entering the adsorption subsystem;

In the actual production of steel enterprises, the original amount of flue gas generated in each flue gas emission process and the pollutant content in the flue gas change. Therefore, the original flue gas flow rate entering each adsorption subsystem and the pollutant content in the flue gas are also in actual production. change according to the difference of By presetting the detection device of each adsorption subsystem, data of the original flue gas flow rate of each adsorption subsystem and the contaminant content in the flue gas can be collected. In addition, since the original flue gas flow rate entering each adsorption subsystem and the pollutant content in the flue gas are important factors affecting the flue gas purification effect, the present invention uses this as the main data for controlling the activated carbon flow rate of each adsorption subsystem. do.

On the adsorption subsystem side, this embodiment ensures the flue gas purification effect and improves the activated carbon utilization rate by accurately controlling the activated carbon flow rate of each adsorption subsystem based on the original flue gas flow rate and the contaminant content in the flue gas.

Step 220, obtaining a flow rate of pollutants in the original flue gas based on the original flue gas flow rate and a pollutant content in the flue gas;

In step 220, the present invention provides a preferred calculation method. For example, if the contaminants are SO ₂ and NO _X , the calculation is specifically to calculate the flow rate of the contaminants in the original flue gas according to the following equation,

는 각 흡착 서브 시스템에 진입하는 원래의 연도가스 중의 오염물 SO₂의 유량, kg/h이고; here

_{is the flow rate of contaminant SO 2} in the original flue gas entering each adsorption subsystem, kg/h;

는 각 흡착 서브 시스템에 진입하는 원래의 연도가스 중의 오염물 SO₂의 함량, mg/Nm³이며;

_{is the content of contaminant SO 2} in the original flue gas entering each adsorption subsystem, mg/Nm ³ ;

는 각 흡착 서브 시스템에 진입하는 원래의 연도가스 중의 오염물 NO_X의 유량, kg/h이고;

_{is the flow rate of pollutant NO X} in the original flue gas entering each adsorption subsystem, kg/h;

는 각 흡착 서브 시스템에 진입하는 원래의 연도가스 중의 오염물 NO_X의 함량, mg/Nm³이며;

_{is the content of contaminant NO X} in the original flue gas entering each adsorption subsystem, mg/Nm ³ ;

는 각 흡착 서브 시스템에 진입하는 원래의 연도가스 유량, Nm³/h이고;

is the original flue gas flow rate entering each adsorption subsystem, Nm ³ /h;

i is the sequence number of the process in which each adsorption subsystem is located.

Step 230, determine the theoretical flow rate of the activated carbon of the adsorption subsystem according to the flow rate of the contaminants in the original flue gas, and determine the theoretical flow rate of the activated carbon of the adsorption subsystem as a real-time flow rate.

In step 230, the present invention provides a preferred calculation method. For example, if contaminants are SO ₂ and NO _X , this calculation is specifically calculated according to the following equation to obtain the theoretical flow rate of activated carbon of the concentrated desorption subsystem and the corresponding adsorption subsystem according to the following equation. confirmed, but

는 각 흡착 서브 시스템의 활성탄의 이론적 유량, kg/h이고; here

is the theoretical flow rate of activated carbon in each adsorption subsystem, kg/h;

K ₁ is a constant and generally takes 15-21; K ₂ is a constant and generally takes 3-4.

This example accurately and quantitatively calculates the theoretical flow rate of activated carbon in each adsorption subsystem based on the original flue gas flow rate and the contaminant content in the flue gas, and is based on data in realizing accurate control of the flue gas purification system of the present invention. provides

Based on the embodiment shown in FIG. 5, in some other embodiments of the present invention, the control method of the present invention further includes the following steps.

Step 140, according to the theoretical flow rate of activated carbon in each adsorption subsystem, set the operating parameters of the material intake device and the material discharge device of each absorption subsystem to realize accurate control for each absorption subsystem.

In the present invention, the time required for the intensive desorption subsystem to be installed in the sintering process and for the contaminated activated carbon to circulate from the adsorption subsystem to the intensive desorption subsystem of the sintering process can be approximated to zero. Therefore, as a preferred embodiment of the present invention on the basis of the above-described embodiment shown in FIG. 5, the theoretical equilibrium flow rate of the current visual activated carbon of the centralized desorption subsystem is determined according to the following equation,

Q _{X0 current} ΣQ = _{Xi (ti)}

Q _X1(ti) =Q _X1Current

where Q _X0current is the current visual theoretical equilibrium flow rate of activated carbon in the concentrated desorption subsystem, kg/h;

는 각 흡착 서브 시스템의 t_i시각에서의 활성탄 유량, kg/h이며;

is the activated carbon flow rate, kg/h, at time _{t i} of each adsorption subsystem;

는 소결 공정의 흡착 서브 시스템의 t_i시각에서의 활성탄 유량, kg/h이고;

is the activated carbon flow rate, kg/h, at time _{t i} of the adsorption subsystem of the sintering process;

Q _{X1 present} is the current hourly circulating flow rate of activated carbon in the adsorption subsystem of the sintering process, kg/h.

In this embodiment, the time required for the contaminated activated carbon to circulate from each adsorption subsystem to the concentrated desorption subsystem is cleverly used _{to determine the ti} time corresponding to the current time in each adsorption subsystem, and each adsorption subsystem Accurately determine the theoretical equilibrium flow rate of activated carbon at the current time of the concentrated desorption subsystem based on the activated carbon flow rate at time t _{i, wherein the concentrated desorption subsystem is installed in the sintering process and the contaminated activated carbon is concentrated from the adsorption subsystem of the sintering process} Since the time required to cycle to the desorption subsystem is 0, the time t1 and the current time are the same, that is, t1 = t _present .

In the present invention, the material intake device, the material discharge device and the material dispensing device of the centralized desorption subsystem include at least a motor and a material transport member driven by the motor, for example, a roller type material feeder. Here, the motor is driven by the converter, and the operating frequency of the converter determines the rotation speed of the motor, and the material transport flow rate of the material intake device, the material discharge device, and the material distribution device are directly proportional to the rotation speed of the motor.

Based on this, in the preferred embodiment shown in FIG. 6 of the present invention, based on the current theoretical activated carbon equilibrium flow rate of the concentrated desorption subsystem, the operating parameters of the material intake device and the material discharge device of the concentrated desorption subsystem are set according to the following steps do.

Step 310, determining the theoretical flow rates of the material intake device and the material discharge device of the centralized desorption subsystem based on the current visual theoretical equilibrium flow rate of the activated carbon of the centralized desorption subsystem;

Optionally, in the step 310, the theoretical flow rate of the material intake device and the material discharge device of the centralized desorption subsystem is determined according to the following equation,

Q ₀ = Q _{0 binary times = Q X0 (t) × j} ;

where Q ₀ is the theoretical flow rate of the mass intake device of the concentrated desorption subsystem, kg/h;

Q _{0 times} is the theoretical flow rate of the mass ejection device of the concentrated desorption subsystem, kg/h;

j is a constant, usually 0.9 to 0.97;

.What should be explained is that since the contaminated activated carbon is activated carbon that has adsorbed a large amount of contaminants, the weight of the contaminated activated carbon of a certain volume is usually increased by 3% to 10% compared to the activated activated carbon of the same volume, or the activated carbon of the same group is desorbed and activated. The weight is 0.9 to 0.97 of the weight after adsorbing the contaminants. Thus, it based the present invention has the following equivalence relations of: current concentration desorption subsystem theoretical flow rate Q _{0 Jean} = concentration desorption theoretical flow rate Q _{0 times} = concentration desorption subsystems of the material discharge apparatus of the subsystems of the material inlet device Theoretical Equilibrium Flow Rate of Visual Activated Carbon

.

Step 320, determining theoretical operating frequencies of the material taking-in device and the material-discharging device according to the theoretical flow rates of the material feeding device and the material discharging device;

In the present invention, the material taking-in device and the material-discharging device of the centralized desorption subsystem can actually realize their material-in and material-discharge functions by using a material transport member driven by a motor. The motor is driven by the converter, and the frequency of the converter determines the rotation speed of the motor, and the re-material transport flow rate of the material intake device and the material discharge device is directly proportional to the rotation speed of the motor, that is, the frequency of the material intake device and the material discharge device is converted. One operating frequency is directly proportional to the mass transport flow rate of the mass transport member. Therefore, optionally, the present invention determines the theoretical operating frequency of the material intake device and the material discharge device according to the following equation,

f _binary =Q _binary /K _binary

f _times =Q _{times 0} /K _times

Where f is theoretically _true operating frequency of the material inlet of the concentration unit and the detachable subsystem;

f _times the theoretical operating frequency of the material discharge apparatus of the focus subsystem and desorption;

K _true and K _times are constants and the unit is kg/(h Hz).

In step 330, the given frequencies of the material taking-in device and the material-discharging device are set according to the theoretical operating frequencies of the material taking-in device and the material-discharging device.

By setting the given frequencies of the material taking-in device and the material-discharging device, when the actual operating frequency of the material feeding device and the material discharging device and their theoretical operating frequency agree with each other, the circulating flow rate of activated carbon in the centralized desorption subsystem is equal to the theoretical equilibrium flow rate of the activated carbon to realize an equilibrium between the concentrated desorption subsystem and each adsorption subsystem.

This embodiment can accurately calculate the theoretical operating frequency according to the theoretical flow rate based on the quantitative relationship between the theoretical operating frequency and the theoretical flow rate of the material taking-in device and the material-discharging device, and use the given operating frequency of the material feeding device and the material discharging device By adjusting the theoretical operating frequency, it achieves the purpose of controlling the mass inlet flow rate and the mass outlet flow rate of the centralized desorption subsystem, and realizes accurate control of the flue gas purification system.

In the present invention, the activated activated carbon discharged from the centralized desorption subsystem is first distributed to each adsorption subsystem through a material distribution device, and then transported to each adsorption subsystem by the transport subsystem. Specifically, on the basis of the above embodiment, FIG. 7 of the present invention shows a preferred embodiment, in which the first material is distributed according to the following steps based on the activated carbon flow rate at time _{t i of the adsorption subsystem of the sintering process.} set operating parameters of the member and the second material dispensing member,

Step 410, determining the material dispensing flow rate of the first material dispensing member according to the _{equation Q min1(t)} =Q _X1(t)×j;

Step 420, determining a theoretical operating frequency of the first material dispensing member according to the material dispensing flow rate of the first material dispensing member;

Step 430, setting a given frequency of the first material dispensing member according to the theoretical operating frequency of the first material dispensing member, and setting the given frequency of the second material dispensing member to a maximum;

where Q _{min 1(t)} is the mass distribution flow rate of the first material distribution member, kg/h.

It should be explained that the first material dispensing member and the second material dispensing member are both a material transport member driven by a motor, for example, a roller type material feeder. control the material transport flow rate, that is, the material distribution flow rate of the material dispensing member.

The embodiment shown in Fig. 7 determines a given frequency according to the theoretical operating frequency based on the quantitative relationship between the theoretical operating frequency of the first material dispensing member and the material dispensing flow rate, and sets the given frequency of the first material dispensing member to the theoretical operating frequency. By adjusting the frequency, the purpose of controlling the activated carbon flow rate of the adsorption subsystem of the sintering process is reached, and at the same time, the given frequency of the second material distribution member is adjusted to the maximum, thereby simplifying the calculation and control steps and improving the stability of the flue gas purification system. ensure operation.

By setting the operating parameters of the material distribution device, the activated carbon is distributed in advance, and then the activated carbon distributed through the transport subsystem is transported to the corresponding adsorption subsystem to save transportation resources, and at the same time, the activated carbon is delivered to the adsorption subsystem. It prevents accumulating and occupying space and prevents the activated carbon from being unsatisfied and affecting the operation of the system.

As can be seen from the structure, operation principle and operation process of the multi-process flue gas purification system, the concentrated desorption subsystem 200 further includes a contaminated activated carbon warehouse 205 for storing the contaminated activated carbon, the contaminated activated carbon storage ( 205) A first unloading device 206 for controlling the unloading flow rate of the contaminated activated carbon is installed at the bottom.

Based on this, the control method of the multi-process flue gas purification system provided in the embodiment of the present invention further includes the following steps on the basis of the steps S110 to S130.

The concentration desorption based on the flow rate of the activated carbon from sub-system of the present time and the adsorption of activated carbon theoretical equilibrium flow rate subsystem of the sintering process of the time t _i and sets the operating parameters of the first unloading device.

Specifically, determine the unloading flow rate at the current time of the first unloading device according to the expression Q _{C0 present} =Q _{X0 present} -Q _{X1 present;}

setting an operating parameter of the unloading device according to the unloading flow rate of the first unloading device;

Here, Q _{C0 current} is the unloading flow rate at the current time of the first unloading device, kg/h.

Actually, in the present invention, the material intake device and the material discharge device of the centralized desorption subsystem are critical devices for controlling the flow rate of the activated carbon of the centralized desorption subsystem. On this basis, in order to ensure that the stable operation of the centralized desorption subsystem is further ensured, the present invention further controls the unloading flow rate of the first unloading device so that the material loading device of the centralized desorption subsystem is insufficient or Or it can prevent the material loading too much situation from occurring.

It should be noted that, as can be seen with reference to FIG. 4 , the centralized desorption subsystem 200 includes the vibrating body 209 installed below the material discharge device 203 of the centralized desorption subsystem and the contaminated activated carbon storage 205 above. It further includes a new additional activated carbon warehouse 207 and a second unloading device 208 installed in to control the unloading flow of

Based on this, the control method of the multi-process flue gas purification system provided in the embodiment of the present invention further includes the following steps on the basis of the steps S110 to S130.

An operating parameter of the second unloading device is set based on the consumed activated carbon flow rate selected by the vibrating body.

Specifically, the flow rate of the new additional activated carbon is determined based on the flow rate of the consumed activated carbon selected by the vibrating body. For example, the flow rate of the consumed activated carbon and the added flow rate of the new additional activated carbon are the same, so that the material input amount and the material of the centralized desorption subsystem Ensure that the emissions are balanced with each other.

Again, an operating parameter of the second unloading device is set based on the addition flow rate of the newly added activated carbon.

In summary, the multi-process flue gas purification system and the control method thereof provided in the embodiment of the present invention provide a concentrated desorption sub-system in the sintering process to form an integrated structure with the adsorption sub-system of the sintering process. Activated carbon circulating between the sub-system and the adsorption subsystem of the sintering process can complete the circulation through the transport device group, thereby saving transport resources as there is no need for additional transport equipment and, at the same time, reduce the impact. By installing a material distribution device in the centralized desorption subsystem, the activated carbon is distributed to the adsorption subsystem of the sintering process through the first material distribution member, and the activated carbon flow rate of the concentrated desorption subsystem and the adsorption subsystem of the sintering process and the remaining adsorption subsystem For the equilibrium relationship between the centralized desorption subsystem and the adsorption subsystem on the centralized desorption subsystem side by making the activated carbon flow rates equalize with each other, and setting the operating parameters of the material intake device, the material discharge device and the material distribution device of the concentrated desorption subsystem Accurate control is realized.

In a specific implementation, the present invention further provides a computer storage medium, wherein a program can be stored in the computer storage medium, and when the program is executed, some or all steps in each embodiment of the control method provided by the present invention are performed. may include The above-described storage medium may be a disk, CD-ROM, read-only memory (English: read-only memory, abbreviation: ROM), or random access memory (English: random access memory, abbreviation: RAM).

Those of ordinary skill in the art to which the present invention pertains can clearly see that the technology in the embodiments of the present invention can be realized in software by adding an essential general hardware platform. Based on this understanding, the technical solutions in the embodiments of the present invention may be implemented in the form of a software product essentially or a part contributing to the prior art. Stored in a medium and including some instructions, it is possible to cause a single computer device (such as a personal computer, a server or a network device) to perform each embodiment of the present invention or a method described in any part of the embodiments.

In this specification, the same or similar parts between the respective embodiments may refer to each other. In particular, in the embodiment, since it is basically similar to the method embodiment, it has been described relatively simply. For related parts, refer to the description in the method embodiment.

The embodiments of the present invention described above do not limit the protection scope of the present invention.

Claims (13)

A multi-process flue gas purification system comprising a plurality of adsorption subsystems respectively installed in each flue gas discharge process, a concentrated desorption subsystem corresponding to the plurality of adsorption subsystems, and a transport subsystem, wherein the adsorption subsystem comprises an adsorption tower; a material introduction device for transporting the activated activated carbon to the adsorption tower and a material discharge device for discharging the contaminated activated carbon in the adsorption tower, wherein the concentrated desorption subsystem includes a desorption activation tower, a material introduction device for transporting the contaminated activated carbon to the desorption activation tower and A multi-process flue gas purification system comprising a material discharging device for discharging activated activated carbon in a desorption activation tower,
the centralized desorption subsystem is installed in a sintering process that is one of the respective flue gas discharge processes;
The centralized desorption subsystem,
at least a first material distribution member for distributing the activated activated carbon to the adsorption subsystem of the sintering process, and a second material distribution member distributing the remaining activated carbon to the adsorption subsystem of the other process; a material distribution device for equilibrating the flow rate and the activated carbon flow rate of the adsorption subsystem of the sintering process and the adsorption subsystem of other processes;
The contaminated activated carbon discharged by the adsorption subsystem of the sintering process is transported to the top buffer warehouse of the centralized desorption subsystem, and the activated activated carbon distributed by the first material distribution member is transferred to the top buffer warehouse of the absorption subsystem of the sintering process. A group of transport devices for transporting; further comprising,
The transport subsystem transports the contaminated activated carbon discharged by the adsorption subsystem of the process other than the sintering process to the centralized desorption subsystem for intensive activation treatment, and transports the activated activated carbon unloaded by the second material distribution member A multi-process flue gas purification system, characterized in that each is transported to an adsorption subsystem of a process other than the sintering process. According to claim 1,
The centralized desorption subsystem,
a contaminated activated carbon warehouse for storing the contaminated activated carbon discharged by the adsorption subsystem; and
A multi-process flue gas purification system, characterized in that it further comprises a first unloading device for unloading the contaminated activated carbon in the contaminated activated carbon warehouse to the below-tower conveying device. 3. The method of claim 1 or 2,
The centralized desorption subsystem,
a vibrating body installed under the material discharging device of the desorption subsystem to separate the spent activated carbon in the activated activated carbon;
A new additional activated carbon warehouse and a second unloading device installed above the contaminated activated carbon warehouse; further comprising,
The second unloading device is a multi-process flue gas purification system, characterized in that for unloading the activated carbon in the newly added activated carbon warehouse to the contaminated activated carbon warehouse. In the control method of the multi-process flue gas purification system, which is the flue gas purification system of claim 1,
determining a real-time flow rate of activated carbon in an adsorption subsystem corresponding to the concentrated desorption subsystem;
determining the theoretical equilibrium flow rate of the activated carbon at the current time of the concentrated desorption subsystem based on the flow rate of the activated carbon at the time _{t i} of each adsorption subsystem _{, wherein the time difference between the time t i} and the current time is that the contaminated activated carbon is transferred to each adsorption sub-system the time required to cycle from the system to the concentrated desorption subsystem;
Based on the theoretical equilibrium flow rate of the activated carbon at the current time of the concentrated desorption subsystem, the operating parameters of the material intake device and the material discharge device of the concentrated desorption subsystem are set, and the activated carbon flow rate at the time _{t i of the adsorption subsystem of the sintering process} realizing control over the flue gas purification system by setting operating parameters of the first material distribution member and the second material distribution member based on control method. 5. The method of claim 4,
obtaining an original flue gas flow rate entering the adsorption subsystem and a contaminant content in the flue gas;
obtaining a flow rate of a pollutant in the original flue gas based on the original flue gas flow rate and a pollutant content in the flue gas;
according to the flow rate of the contaminants in the original flue gas, determining the theoretical flow rate of the activated carbon of the adsorption subsystem, and determining the theoretical flow rate of the activated carbon of the adsorption subsystem as a real-time flow rate; corresponding to the centralized desorption subsystem according to A control method of a multi-process flue gas purification system, characterized in that the real-time flow rate of activated carbon of the adsorption subsystem is determined. 6. The method of claim 5,
Calculate the flow rate of pollutants in the original flue gas according to the following equation based on the original flue gas flow rate and the pollutant content in the flue gas,

here

_{is the flow rate of contaminant SO 2} in the original flue gas entering each adsorption subsystem, kg/h;

_{is the content of contaminant SO 2} in the original flue gas entering the adsorption subsystem, mg/Nm ³ ;

_{is the flow rate of pollutant NO X} in the original flue gas entering the adsorption subsystem, kg/h;

_{is the content of pollutant NO X} in the original flue gas entering the adsorption subsystem, mg/Nm ³ ;

is the original flue gas flow rate entering the adsorption subsystem, Nm ³ /h;
i is the sequence number of the process in which the adsorption subsystem is located;
Determine the theoretical flow rate of activated carbon in the adsorption subsystem according to the following equation based on the flow rate of contaminants in the original flue gas,

here

is the theoretical flow rate of activated carbon in the adsorption subsystem, kg/h;
K ₁ is a constant and generally takes 15-21; K ₂ is a constant, characterized in that generally taking 3-4, a control method of a multi-process flue gas purification system. 7. The method of claim 6,
_{Based on the activated carbon flow rate at the time t i} of the adsorption subsystem, determine the theoretical equilibrium flow rate of the activated carbon at the current time of the concentrated desorption subsystem according to the following equation,
Q _{X0 current} ΣQ = _{Xi (ti)}
Q _X1(ti) =Q _X1Current
where Q _X0current is the current visual theoretical equilibrium flow rate of activated carbon in the concentrated desorption subsystem, kg/h;

is the activated carbon flow rate, kg/h, at time _{t i} of the adsorption subsystem corresponding to the concentrated desorption subsystem;

is the activated carbon flow rate, kg/h, at time _{t i} of the adsorption subsystem of the sintering process;
Q _{X1 Current} is the current time circulating flow rate of activated carbon of the adsorption subsystem of the sintering process, kg/h, A control method of a multi-process flue gas purification system. 8. The method of claim 6 or 7,
Control method of a multi-process flue gas purification system, characterized in that, based on the theoretical equilibrium flow rate of the activated carbon at the present time of the centralized desorption subsystem, the operating parameters of the material intake device and the material discharge device of the centralized desorption subsystem are set according to the following steps :
determining the theoretical flow rates of the material intake device and the material discharge device of the concentrated desorption subsystem based on the current visual theoretical equilibrium flow rate of the activated carbon of the concentrated desorption subsystem;
determining theoretical operating frequencies of the material taking-in device and the material-discharging device according to the theoretical flow rates of the material-injecting device and the material-discharging device;
setting a given frequency of the material withdrawing device and the material ejecting device based on the theoretical operating frequencies of the material taking-in device and the material-discharging device. 9. The method of claim 8,
Determine the theoretical flow rates of the material intake device and the material discharge device of the centralized desorption subsystem according to the following equation,
Q ₀ = Q _{0 binary times = Q X0 (t) × j} ;
where Q ₀ is the theoretical flow rate of the mass intake device of the desorption subsystem, kg/h;
Q _{0 times} is the theoretical flow rate of the mass ejection device of the desorption subsystem, kg/h;
j is a constant, usually 0.9 to 0.97;
Determine the theoretical operating frequency of the material intake device and the material discharge device according to the following equation,
f _binary =Q _binary /K _binary
f _times =Q _{times 0} /K _times
Where f is theoretically _true operating frequency of the material inlet of the concentration unit and the detachable subsystem;
f _times the theoretical operating frequency of the material discharge apparatus of the focus subsystem and desorption;
K and K _{binary vessel,} the process control method of the flue gas purification system, characterized in that constant. 10. The method of claim 9,
Based on the activated carbon flow rate at time _{t i} of the adsorption subsystem of the sintering process,
determining a material distribution flow rate of the first material distribution member based on the equation Q _min1(t) =Q _X1(t)×j;
determining a theoretical operating frequency of the first material dispensing member based on the material dispensing flow rate of the first material dispensing member;
setting a given frequency of the first material dispensing member based on the theoretical operating frequency of the first material dispensing member; and
setting the operating parameters of the first material dispensing member and the second material dispensing member according to; setting a given frequency of the second material dispensing member to a maximum;
Wherein Q _{min 1 (t)} is the mass distribution flow rate of the first material distribution member, kg/h, the control method of the multi-process flue gas purification system, characterized in that. 7. The method of claim 5 or 6,
according to the theoretical flow rate of the activated carbon of the adsorption subsystem, by setting the operating parameters of the mass intake device and the mass discharge device of the adsorption subsystem to realize accurate control for each adsorption subsystem; Control method of process flue gas purification system. In the control method of the multi-process flue gas purification system which is the flue gas purification system of claim 2,
determining a real-time flow rate of activated carbon in an adsorption subsystem corresponding to the concentrated desorption subsystem;
determining the theoretical equilibrium flow rate of the activated carbon at a current time of the concentrated desorption subsystem based on the flow rate of the activated carbon at the time _{t i} of each adsorption subsystem _{, wherein the time difference between the time t i} and the current time causes the contaminated activated carbon to be transferred to each adsorption subsystem the time required to cycle from to the concentrated desorption subsystem;
setting operation parameters of the material intake device and the material discharge device of the concentrated desorption subsystem based on the theoretical equilibrium flow rate of the activated carbon at the present time of the concentrated desorption subsystem;
setting operating parameters of the first material distribution member and the second material distribution member based on the activated carbon flow rate at time _{t i} of the adsorption subsystem of the sintering process; and
Control of the flue gas purification system by setting the operating parameters of the first unloading device based on the theoretical equilibrium flow rate of the activated carbon at the current time of the centralized desorption subsystem and _{the activated carbon flow rate at the time t i of the adsorption subsystem of the sintering process} A control method of a multi-process flue gas purification system comprising the step of realizing a. In the control method of the multi-process flue gas purification system, which is the flue gas purification system of claim 3,
determining a real-time flow rate of activated carbon in an adsorption subsystem corresponding to the concentrated desorption subsystem;
determining the theoretical equilibrium flow rate of the activated carbon at a current time of the concentrated desorption subsystem based on the flow rate of the activated carbon at the time _{t i} of each adsorption subsystem _{, wherein the time difference between the time t i} and the current time causes the contaminated activated carbon to be transferred to each adsorption subsystem the time required to cycle from to the concentrated desorption subsystem;
setting operation parameters of the material intake device and the material discharge device of the concentrated desorption subsystem based on the theoretical equilibrium flow rate of the activated carbon at the present time of the concentrated desorption subsystem;
setting operating parameters of the first material distribution member and the second material distribution member based on the activated carbon flow rate at time _{t i} of the adsorption subsystem of the sintering process; and
and realizing control of the flue gas purification system by setting an operating parameter of the second unloading device based on the consumed activated carbon flow rate selected by the vibrating body. control method.

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