CN112619356A - Automatic control device for flue gas balance system of active coke adsorption tower - Google Patents

Automatic control device for flue gas balance system of active coke adsorption tower Download PDF

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Publication number
CN112619356A
CN112619356A CN202011437374.1A CN202011437374A CN112619356A CN 112619356 A CN112619356 A CN 112619356A CN 202011437374 A CN202011437374 A CN 202011437374A CN 112619356 A CN112619356 A CN 112619356A
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adsorption unit
flue gas
adsorption
pressure
outlet
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王志国
寿宏飚
徐健
付柏淋
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MCC North Dalian Engineering Technology Co Ltd
Northern Engineering and Technology Corp MCC
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MCC North Dalian Engineering Technology Co Ltd
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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
    • 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
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/404—Further details for adsorption processes and devices using four beds

Abstract

The invention belongs to the field of automatic control of environmental-friendly production, and particularly relates to an automatic control device of an active coke adsorption tower flue gas balance system, which is characterized by comprising a gas flowmeter and a flow transmitter which are arranged on an outlet main pipe of a booster fan, a pressure transmitter on an inlet branch pipe of an inlet chamber of each adsorption unit, a pressure transmitter and a thermal resistor of a transition gas chamber of each adsorption unit, a pressure transmitter on an outlet branch pipe of an outlet chamber of each adsorption unit, and an electric butterfly valve on an outlet branch pipe of the outlet chamber of each adsorption unit, wherein the pressure transmitters, the thermal resistors and the electric butterfly valves on different positions of each adsorption unit are connected with a PLC system. The method is not influenced by the steps of processing, manufacturing, assembling, welding and the like of elements of each adsorption unit, and realizes the measurement of the resistance coefficient zeta of each adsorption unit under the actual production working condition, thereby obtaining the flue gas flow of each adsorption unit, controlling the flue gas flow by adjusting the electric butterfly valve at the outlet, and really realizing the automatic control of the tower-attached flue gas balance system.

Description

Automatic control device for flue gas balance system of active coke adsorption tower
Technical Field
The invention belongs to the field of automatic control of environmental-friendly production, and particularly relates to an automatic control device for a flue gas balance system of an active coke adsorption tower.
Background
Along with the ultra-low of industrial flue gasThe implementation of emission standard, flue gas purification system has gradually become sintering, the indispensable process of thermoelectricity, and flue gas purification mainly has dry method, semi-dry method and wet flue gas desulfurization technology at present. In recent years, active coke-drying desulfurization is more and more emphasized, and the process becomes the preferred scheme of the flue gas purification method. In the engineering of active coke flue gas purification, the adsorption tower is the core equipment, because the flue gas purification is completed in the adsorption unit of the adsorption tower, the flue gas is fully contacted with the active coke in the adsorption unit, and the SO in the flue gas is absorbed by the adsorbability of the active coke2，NOXAnd dust and the like are adsorbed to finish the flue gas purification. Because the sintering flue gas volume is bigger, normal adsorption tower all comprises a plurality of independent parallel adsorption units, and the flue gas divides into the multichannel and corresponds each adsorption unit by all the way, SO in the flue gas2，NOXPollutants such as dust and the like are adsorbed by the activated carbon layer or generate harmless substances through catalytic reaction, and the flue gas purification is completed in each adsorption unit. Multiple field feedbacks can cause the pollutant in the purified flue gas to exceed the standard when the flue gas entering each adsorption unit is unbalanced, and an operator can only adjust the opening of the outlet valve of each adsorption unit according to experience, and can only observe the change of the pressure difference value of the inlet and the outlet of the adsorption unit after adjustment, but whether the balance is achieved is not clear, especially in SO2Or NOXWhen the discharge exceeds the standard, the adsorption unit cannot be adjusted clearly, and the adjustment can be attempted only by experience, so that troubles are brought to actual operators, the discharge exceeding time is too long, and even the phenomenon of production halt and pause required by the environmental protection bureau occurs.
Therefore, it is very important to balance the flue gas entering each adsorption unit of the adsorption tower, and the current situation is that the opening degree of the outlet valve can be manually adjusted by experience only by looking at the difference value of the inlet pressure and the outlet pressure of each adsorption unit, sometimes the inlet pressure and the outlet pressure of each adsorption unit are the same, but the flue gas is unbalanced (the emission exceeds the standard), so that great pressure and confusion are brought to actual production, and therefore, the development of the automatic control device of the flue gas balance system of the active coke adsorption tower in an online and real-time manner has important practical significance and value.
Disclosure of Invention
The invention aims to provide an automatic control device for a flue gas balance system of an active coke adsorption tower, which solves the problem of slow operation and adjustment after the flue gas of each adsorption unit among adsorption towers is unbalanced, can improve the production rate of a purification system, shortens the time of abnormal emission exceeding the standard, and ensures that the flue gas purification system runs stably and efficiently.
The purpose of the invention is realized by the following technical scheme:
the invention discloses an automatic control device of an active coke adsorption tower flue gas balance system, which is characterized by comprising a gas flowmeter and a flow transmitter which are arranged on an outlet main pipe of a booster fan, a pressure transmitter which is respectively arranged on an inlet branch pipe of an inlet chamber of each adsorption unit, a pressure transmitter and a thermal resistor which are respectively arranged on a transition gas chamber of each adsorption unit, a pressure transmitter which is respectively arranged on an outlet branch pipe of an outlet chamber of each adsorption unit, and an electric butterfly valve which is respectively arranged on an outlet branch pipe of the outlet chamber of each adsorption unit, wherein the pressure transmitter, the thermal resistor and the electric butterfly valve at different positions of each adsorption unit are connected with a PLC system.
The PLC system measures the resistance coefficient zeta of each adsorption unit, the measured air quantity, inlet and outlet pressure, transition air chamber pressure and temperature are processed by the adsorption tower, and the resistance coefficient zeta of the first adsorption unit is actually measured according to a formula seven1Then, there are:
Figure BDA0002829573990000021
QsheetLambda air flow (m) through the adsorption unit per unit time3/h)；
S1Lambda effective area of the grate plate at the inlet side of the first coke bed in the first adsorption unit (m)2)；
P11Pressure PT-11(Pa) at inlet of Lambda 1 adsorption unit;
P12pressure PT-12(Pa) at the outlet of the Lambda 1 adsorption unit;
P13the pressure PT-13(Pa) of the Lambda 1 adsorption unit transition air chamber;
T11the temperature TE-11 (DEG C) of the Lambda 1 adsorption unit transition gas chamber;
P0Λ local standard atmospheric pressure (typically 101325) (Pa);
ρsign boardThe density of the flue gas under the lambda standard state (generally 1.29) (Kg/m)3)；
g Λ local acceleration of gravity (typically 9.8) (m/s)2)；
Respectively measuring the resistance coefficients zeta of the second, third and fourth adsorption units according to the steps2/ζ3/ζ4And completing the measurement of the resistance coefficient of each adsorption unit, and endowing the resistance coefficient of each adsorption unit to a flow velocity calculation formula V corresponding to the PLC, wherein the flow velocity calculation formula V comprises the following steps:
Figure BDA0002829573990000031
wherein x is the number of the corresponding adsorption unit.
The invention has the advantages that:
(1) the automatic control device of the flue gas balance system of the active coke adsorption tower is not influenced by the steps of processing, manufacturing, assembling, welding and the like of elements of each adsorption unit, and the resistance coefficient zeta of each adsorption unit is measured under the condition of actual production working conditions;
(2) according to the automatic control device for the flue gas balance system of the active coke adsorption tower, the flow velocity in the adsorption unit is calculated according to related data, a flowmeter is not required to be arranged, the occupied area is small, the investment is low, and the application range is wider (new construction or old project modification);
(3) the automatic control device of the flue gas balance system of the active coke adsorption tower realizes the same flow velocity of the flue gas in each adsorption unit (in a stable area), and the adsorption tower realizes self-adaptation to the amount of the flue gas to be treated.
Drawings
FIG. 1 is a flow chart of the flue gas balance control process of the adsorption tower of the present invention.
FIG. 2 is a schematic view of the distribution of the flue gas direction in the adsorption unit of the present invention.
Detailed Description
The following further describes the embodiments of the present invention with reference to the drawings.
As shown in figures 1 and 2, the automatic control device of the flue gas balance system of the active coke adsorption tower is characterized by comprising a gas flow meter FE-10 and a flow transmitter FT-10 which are arranged on an outlet header pipe of a booster fan 1, pressure transmitters PT-11, PT-21, PT-31 and PT-41 which are respectively arranged on an inlet branch pipe of an inlet chamber of each adsorption unit, pressure transmitters PT-13, PT-23, PT-33 and PT-43 which are respectively arranged on a transition gas chamber of each adsorption unit, thermal resistors TE-11, TE-21, TE-31 and TE-41 which are respectively arranged on an outlet branch pipe of an outlet chamber of each adsorption unit, a pressure transmitter PT-12, a PT-22, a PT-32 and a PT-42 which are respectively arranged on an outlet branch pipe of the outlet chamber of each adsorption unit, an electric motor-driven HV/HZ-11, a butterfly valve and, HV/HZ-21, HV/HZ-31 and HV/HZ-41, pressure transducers at different locations of each adsorption unit, thermal resistors and electric butterfly valves are connected to PLC system XIC 11.
The PLC system XIC11 measures the resistance coefficient zeta of each adsorption unit, the measured air volume, inlet and outlet pressure, transition air chamber pressure and temperature are processed by the adsorption tower, and the resistance coefficient zeta of the first adsorption unit is actually measured according to a formula seven1Then, there are:
Figure BDA0002829573990000041
QsheetLambda air flow (m) through the adsorption unit per unit time3/h)；
S1Lambda effective area of the grate plate at the inlet side of the first coke bed in the first adsorption unit (m)2)；
P11Pressure PT-11(Pa) at inlet of Lambda 1 adsorption unit;
P12pressure PT-12(Pa) at the outlet of the Lambda 1 adsorption unit;
P13the pressure PT-13(Pa) of the Lambda 1 adsorption unit transition air chamber;
T11the temperature TE-11 (DEG C) of the Lambda 1 adsorption unit transition gas chamber;
P0Λ local standard atmospheric pressure (typically 101325) (Pa);
ρsign boardThe density of the flue gas under the lambda standard state (generally 1.29) (Kg/m)3)；
g Λ local acceleration of gravity (typically 9.8) (m/s)2)；
Respectively measuring the resistance coefficients zeta of the second, third and fourth adsorption units according to the steps2/ζ3/ζ4And completing the measurement of the resistance coefficient of each adsorption unit, and endowing the resistance coefficient of each adsorption unit to a flow velocity calculation formula V corresponding to the PLC, wherein the flow velocity calculation formula V comprises the following steps:
Figure BDA0002829573990000051
wherein x is the number of the corresponding adsorption unit.
The automatic control device of the flue gas balance system of the active coke adsorption tower realizes the flow uniformity of desulfurization and dust removal by the flue gas passing through a solid barrier based on the adsorption tower and the bag-type dust remover, and the pressure loss formula of the bag-type dust remover comprises the following components:
Figure BDA0002829573990000052
pressure loss (mmH) of Δ P Λ adsorption unit2O)；
The drag coefficient of the zeta Λ adsorption unit;
ρworker's toolLambda gas density (Kg/m) at operating temperature and pressure3)；
V Λ is the gas flow velocity (m/s) through the adsorption unit;
g Λ gravity acceleration (m/s)2)；
The gas flow velocity V through the adsorption column can be found according to the formula one:
Figure BDA0002829573990000053
according to a density calculation formula:
Figure BDA0002829573990000054
ρworker's toolLambda gas density (Kg/m) at operating temperature and pressure3)；
ρSign boardLambda Standard State gas Density (Kg/m)3)；
TMeasuringLambda the temperature of the flue gas in the adsorption unit (DEG C);
PmeasuringΛ pressure (Pa) of flue gas within the adsorption unit;
P0Λ local atmospheric pressure (Pa);
according to the trend of the flue gas in the adsorption unit, the pressure loss delta P of the flue gas in the adsorption unit is the difference between the inlet pressure of the adsorption unit and the outlet pressure of the adsorption unit, namely:
Figure BDA0002829573990000061
P1lambda the pressure (Pa) of the flue gas at the inlet of the adsorption unit;
P2the pressure (Pa) of the lambda flue gas at the outlet of the adsorption unit;
pressure loss (mmH) of Δ P Λ adsorption unit2O)；
Substituting the formula four and the formula three into the formula two, the following results are obtained:
Figure BDA0002829573990000062
with reference to fig. 1 (flow chart of flue gas balance control process of adsorption tower), it can be seen that the flow velocity V of flue gas passing through the adsorption unit is pre-calculated in formula five, other parameters can be obtained by looking up a table or setting an on-line detection device, and only the resistance coefficient ζ of the adsorption unit is reduced, and the manufacturing, construction and assembly of each adsorption unit have more or less certain deviation, so that the actual resistance coefficient of each adsorption unit is deviated, and thus, actual measurement and calibration need to be performed before the normal commissioning of a project (i.e., at the debugging stage), and the actual resistance coefficient ζ of each adsorption unit is calculated.
The specific procedure for measuring the drag coefficient ζ is as follows:
filling each adsorption unit of the adsorption tower with active coke, and operating the active coke according to normal production;
the booster fan 1 is operated, the air quantity is controlled to be the rated operation air quantity of a single adsorption unit, and Q is usedSheetTo represent;
closing the inlet and outlet valves of other adsorption towers in the series, only opening the inlet and outlet valves of one adsorption tower, and recording the air volume and inlet and outlet pressure of the current adsorption tower, the pressure and temperature of a transition air chamber when the operation is stable;
according to the continuous and stable operation characteristics of the flue gas and the relationship between the air quantity and the air speed, the method comprises the following steps:
QsheetEither sxv (six formula)
QSheetLambda air flow (m) through the adsorption unit per unit time3/h)；
The flue gas passes through the cross section area (m) of the active coke in the adsorption unit simultaneously2)；
The V lambda flue gas passes through the flow velocity (m/h) of the adsorption unit;
from the formula five and the formula six, there is an actually measured resistance coefficient ζ formula:
Figure BDA0002829573990000071
namely:
Figure BDA0002829573990000072
repeating the process, and carrying out actual measurement on the actual resistance coefficient zeta of each adsorption unit of the adsorption tower one by one;
the measured resistance coefficient ζ is written into the corresponding formula five, for example, the gas flow rate of the first adsorption unit is:
Figure BDA0002829573990000073
with reference to fig. 1 (flow chart of the flue gas balance control process of the adsorption tower), there are:
P11pressure at inlet of adsorption unit # Λ 1 (corresponding to device PT-11) (Pa);
P12pressure at the outlet of the adsorption unit No. Lambda 1 (corresponding to equipment PT-12) (Pa);
P13the pressure (corresponding to equipment PT-13) (Pa) of a Lambda 1 adsorption unit transition air chamber;
T11the temperature (corresponding to equipment TE-11) of a Lambda 1 adsorption unit transition gas chamber is (DEG C);
ζ1adsorption unit resistance coefficient # 1 (the measured coefficient described above);
P0Λ local standard atmospheric pressure (typically 101325) (Pa);
ρsign boardThe density of the flue gas under the lambda standard state (generally 1.29) (Kg/m)3)；
g Λ local acceleration of gravity (typically 9.8) (m/s)2)；
Therefore, the online real-time flue gas flow rate of each adsorption unit can be obtained through calculation in the PLC system XIC11 (or DCS system), and various functional operations are completed in the PLC system XIC 11.
Firstly, comparing the flue gas flow rate of each adsorption unit with the designed rated flow rate in the adsorption unit, and if the flow rate in the adsorption unit is greater than the designed rated value, giving an alarm on a main control picture;
secondly, sequencing the flue gas flow rates of all the adsorption units, removing a maximum value and a minimum value, and then taking the remaining average value (in the other method, sequencing the flue gas flow rates of the adsorption units, adjacently performing difference, if the difference value is larger than one tenth of the designed rated flow rate, removing the value far away from the average value, recording the value in an alarm table, if the difference value is not larger than the design rated flow rate, considering all the values to be effective, and calculating the average value), wherein the value is used as the target value of the flow rate of each adsorption unit, and the sampling period in the step is larger than the retention time of the flue gas in the adsorption units;
thirdly, in each adsorption unit, the target value obtained by the calculation in the second step is used as a set value for the PID adjustment of the outlet adjusting valve of the adsorption unit, the adsorption unit calculates the flow rate in real time to be used as a feedback value for the PID adjustment of the outlet adjusting valve, and the general stable area is +/-5 of the set value, so that the PID automatic adjustment of the outlet adjusting valve is realized, and the step is real-time.
Therefore, each adsorption unit is adjusted around a target value in each sampling period, and the target value of the next sampling period is changed along with the fluctuation of the smoke volume to be processed, so that the method has certain adaptivity, and the automatic control of the smoke balance of each adsorption unit of the adsorption tower is really realized.
Examples
The adsorption tower of the embodiment of the invention consists of four adsorption units. The method comprises the following steps: the gas flow meter FE-10 and the flow transmitter FT-10 which are arranged on the outlet header pipe of the booster fan 1 realize air volume adjustment by controlling the frequency converter 2 of the booster fan 1, and the invention is mainly used for initial calibration and then on-line correction of the resistance coefficient of each adsorption unit of the adsorption tower. The position is shown in figure 1; the adsorption tower is composed of a plurality of adsorption units, and flue gas passes through a main pipe by a booster fan 1 and then is divided into a plurality of branch pipes corresponding to the adsorption units. Now, the first adsorption unit 3 is taken as an example to describe that the flue gas enters the adsorption unit in the direction and the measuring point arrangement (as shown in fig. 2), an adsorption unit inlet pressure detection pressure transmitter PT-11 is arranged at the position of the branch pipe entering the inlet chamber 8, the flue gas enters the first-stage coke bed 10 through the side grid plate 12 of the first-stage coke bed 10 in the left and right directions from the inlet chamber 8 to start first-stage adsorption, the flue gas enters the transition air chamber 13 through the side grid plate 12 of the first-stage coke bed 10 to give out air, a flue gas temperature detection thermal resistance TE-11 and a pressure detection pressure transmitter PT-13 are arranged in the transition air chamber 13, the flue gas enters the second-stage coke bed 11 through the side grid plate 12 of the second-stage coke bed 11 from the transition air chamber 13 to enter the primary-stage coke bed 11, the flue gas after primary purification contacts with the regenerated active coke layer again to complete secondary adsorption, the purified flue gas enters the outlet chamber 9 through the, after being branched, the water flows into a main pipe and is sent to a chimney 7 for discharge. An adsorption unit outlet pressure detection pressure transmitter PT-12 is arranged at the joint of the air outlet chamber 9 and the branch pipe, and an electric butterfly valve HV/HZ-11 is arranged on the branch pipe to adjust the circulating flue gas in the adsorption unit.
The detection parameters in the above-mentioned equipment table are all sent into a PLC system XIC11 (or a DCS system), and the resistance coefficient zeta of each adsorption unit is measured after the initial stage of project commissioning or the shutdown and overhaul of a plant, and the first adsorption unit is exemplified by the following specific method:
each adsorption unit of the adsorption tower is filled with active coke, and the active coke is operated according to normal production; the booster fan 1 is operated, the air quantity is controlled to be the rated operation air quantity of a single adsorption unit, and Q is usedSheetTo show that the inlet and outlet valves of other adsorption units of the adsorption tower are closed, only the inlet and outlet valves of the first adsorption tower are all opened, and the rotating speed of the booster fan 1 is adjusted by the frequency converter 2, so that the air quantity Q of the FE-10 of the gas flowmeter at the outlet of the booster fan 1 is enabled to be10＝QSheetWhen the operation is stable, recording the current air handling capacity, inlet and outlet pressure, transition air chamber pressure and temperature of the adsorption tower;
according to the seventh formula, the resistance coefficient ζ of the first adsorption unit can be actually measured1Then, there are:
Figure BDA0002829573990000101
QsheetLambda air flow (m) through the adsorption unit per unit time3/h)；
S1Lambda effective area of the grate plate at the inlet side of the first coke bed in the first adsorption unit (m)2)；
P11Pressure PT-11(Pa) at inlet of Lambda 1 adsorption unit;
P12pressure PT-12(Pa) at the outlet of the Lambda 1 adsorption unit;
P13the pressure PT-13(Pa) of the Lambda 1 adsorption unit transition air chamber;
T11the temperature TE-11 (DEG C) of the Lambda 1 adsorption unit transition gas chamber;
P0Λ local standard atmospheric pressure (typically 101325) (Pa);
ρsign boardThe density of the flue gas under the lambda standard state (generally 1.29) (Kg/m)3)；
g Λ local acceleration of gravity (typically 9.8) (m/s)2)；
The resistance coefficients zeta of the second adsorption unit 4, the third adsorption unit 5 and the fourth adsorption unit 6 are respectively measured according to the steps2/ζ3/ζ4And completing the measurement of the resistance coefficient of each adsorption unit, and endowing the resistance coefficient of each adsorption unit to a flow velocity calculation formula V corresponding to the PLC system XIC11 (or DCS system), wherein the flow velocity calculation formula V comprises the following steps:
Figure BDA0002829573990000102
x in the above formula is the number of the corresponding adsorption unit;
the online real-time flue gas flow velocity of each adsorption unit is obtained by calculating the detection parameters of the adsorption units in a PLC system XIC11 (or a DCS system), and various functional operations are completed in a PLC system XIC 11.
Firstly, judging whether the flow rate of the flue gas of the unit is normal or not, and alarming on a main control picture if the flow rate is abnormal;
secondly, setting a large sampling period for controlling the whole flue gas balance of the adsorption tower according to the residence time of the flue gas in the adsorption unit, wherein the large sampling period is generally more than or equal to the residence time of the flue gas in the adsorption unit; judging whether the data of each adsorption unit in the adopted period is valid or not by comparison, and calculating an average value by using the valid data to serve as a target value of the next period;
thirdly, in each adsorption unit, the target value obtained by the calculation in the second step is used as a set value for the PID adjustment of the outlet regulating valve of each adsorption unit, the flow rate of each adsorption unit is calculated in real time and is used as a feedback value for the PID adjustment of the outlet regulating valve, and the general stable area is +/-5 of the set value, so that the PID automatic adjustment of the outlet regulating valve is realized, and the step is real-time.
Therefore, the flue gas flow velocity of each adsorption unit is adjusted around a target value in each large sampling period, and the target value of the next sampling period is changed along with the fluctuation of the flue gas volume to be processed, so that the method has certain adaptivity, and the automatic control of the flue gas balance of each adsorption unit of the adsorption tower is really realized.
The automatic control device of the flue gas balance system of the active coke adsorption tower is not influenced by the steps of processing, manufacturing, assembling, welding and the like of elements of each adsorption unit, and the resistance coefficient zeta of each adsorption unit is measured under the condition of actual production working conditions; the flow velocity in the adsorption unit is calculated according to related data, a flowmeter is not needed, the occupied area is small, the investment is low, and the application range is wider (new construction or old project modification); the flue gas flow velocity in each adsorption unit is the same (in a stable region), and the adsorption tower realizes self-adaptation to the flue gas volume to be processed.
The equipment for setting the measuring point of each adsorption unit is shown in the table I:
watch 1
Figure BDA0002829573990000111
Figure BDA0002829573990000121

Claims (2)

1. The utility model provides an active burnt adsorption tower flue gas balance system automatic control device, its characterized in that is including setting up gas flowmeter and the flow transmitter on booster fan export house steward, set up the pressure transmitter on every adsorption unit inlet chamber entry branch pipe respectively, set up pressure transmitter and the thermal resistance at every adsorption unit transition air chamber respectively, set up the pressure transmitter on every adsorption unit outlet chamber export branch pipe respectively, set up the electric butterfly valve on every adsorption unit outlet chamber export branch pipe respectively, the pressure transmitter on the different positions of each adsorption unit, thermal resistance and electric butterfly valve all are connected with the PLC system.
2. The automatic control device of flue gas balance system of active coke adsorption tower of claim 1, wherein said PLC system measures resistance coefficient ζ of each adsorption unit, measures the air volume processed by the adsorption tower, the inlet and outlet pressure, the transition air chamber pressure and the temperature, and measures the resistance coefficient ζ of the first adsorption unit according to the formula seven1Then, there are:
Figure FDA0002829573980000011
QsheetLambda air flow (m) through the adsorption unit per unit time3/h)；
S1Lambda effective area of the grate plate at the inlet side of the first coke bed in the first adsorption unit (m)2)；
P11Pressure PT-11(Pa) at inlet of Lambda 1 adsorption unit;
P12pressure PT-12(Pa) at the outlet of the Lambda 1 adsorption unit;
P13the pressure PT-13(Pa) of the Lambda 1 adsorption unit transition air chamber;
T11the temperature TE-11 (DEG C) of the Lambda 1 adsorption unit transition gas chamber;
P0Λ local standard atmospheric pressure (typically 101325) (Pa);
ρsign boardThe density of the flue gas under the lambda standard state (generally 1.29) (Kg/m)3)；
g Λ local acceleration of gravity (typically 9.8) (m/s)2)；
Respectively measuring the resistance coefficients zeta of the second, third and fourth adsorption units according to the steps2/ζ3/ζ4And completing the measurement of the resistance coefficient of each adsorption unit, and endowing the resistance coefficient of each adsorption unit to a flow velocity calculation formula V corresponding to the PLC, wherein the flow velocity calculation formula V comprises the following steps:
Figure FDA0002829573980000021
wherein x is the number of the corresponding adsorption unit.
CN202011437374.1A 2020-12-11 2020-12-11 Automatic control device for flue gas balance system of active coke adsorption tower Pending CN112619356A (en)

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Application Number Priority Date Filing Date Title
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