CN102512917B - Control system for renewable flue gas desulfurization system and control method - Google Patents

Control system for renewable flue gas desulfurization system and control method Download PDF

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Publication number
CN102512917B
CN102512917B CN201110416707.7A CN201110416707A CN102512917B CN 102512917 B CN102512917 B CN 102512917B CN 201110416707 A CN201110416707 A CN 201110416707A CN 102512917 B CN102512917 B CN 102512917B
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temperature
control
steam
flow
reboiler
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CN201110416707.7A
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Chinese (zh)
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CN102512917A (en
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赵与峰
何勇
付宏宇
王俭华
罗治秋
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攀钢集团有限公司
攀钢集团攀枝花钢钒有限公司
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Abstract

The invention provides a control system used for a renewable flue gas desulfurization system and a control method. The control system comprises a reboiler temperature control unit and a sulfur dioxide blower control unit, wherein the reboiler temperature control unit comprises a first temperature measuring element, a second temperature element, a cooling device, a steam flow control valve and a first control element; and the sulfur dioxide blower control unit comprises a flow measuring element, a pressure measuring element, a gas flow control valve and a second control element. In the invention, the temperature of the steam in the reboiler can be controlled in the range of a process requirement, so that the scales in the reboiler can be reduced; the heat exchange efficiency and steam utilization rate are improved; the flow and pressure of the gas in the sulfur dioxide blower and an acid-making device can be rationally controlled; and the acid-making process is guaranteed smoothly.

Description

Control system and control method for renewable flue gas desulfurization system

Technical field

The present invention relates to automatic control technology field, more particularly, relate to a kind of control system for renewable flue gas desulfurization system and control method.

Background technology

Reboiler (also claiming reboiler) is the device that liquid is vaporized again by heating.Described heating can be by realizing from the steam of vapour source to reboiler access.In other words, reboiler be one can heat-shift, there is the special heat exchanger of vaporization space simultaneously.

Renewable flue gas desulfurization system is for implementing the device of renewable flue gas desulphurization process.Fig. 1 shows the schematic diagram of the renewable flue gas desulfurization system of prior art.As shown in Figure 1, renewable flue gas desulfurization system generally includes reboiler 10, desorber 20, absorption tower 30 and desorption gas and reclaims acid making system 40.Conventionally, described renewable flue gas desulphurization process can comprise the following steps: first, in absorption tower 30, the desulfuration solution of utilization such as amine liquid or ionic liquid absorbs for example, the oxysulfide gas such as sulfur dioxide and sulfur trioxide in flue gas (comprising the various flue gases that contain oxysulfide or industrial waste gas,, sintered discharge gas, blast furnace gas, coke-stove gas, coal-fired plant boiler waste gas, heating furnace waste gas etc.) and realizes the purification to flue gas; Then, in desorber 20, the oxysulfide gas in Desorption desulphurization liquation at high temperature, to obtain highly purified oxysulfide gas, and the desulfuration solution of the absorption oxysulfide gas ability that is simultaneously restored, desulfuration solution after desorb is provided to again absorption tower and absorbs the oxysulfide gas in flue gas, thereby realizes the circulation of absorption step and desorption procedure.

Reboiler can be connected with the desorber 20 of renewable flue gas desulfurization system, for example, so that the liquid (, the desulfuration solution that contains oxysulfide) that flows into reboiler from desorber 20 is heated to be to steam, thereby promotes the desorb of described liquid in desorber.

Yet, in the prior art, because the vapor (steam) temperature of the vapour source for reboiler is heated is conventionally higher, so cause reboiler incrustation serious, and then cause reduction of heat exchange efficiency and waste of steam, when even serious, will cause reboiler to stop up, thereby affect normally carrying out of producing.

In addition,, if there is large-scale temperature fluctuation for the high-temperature steam of vapour source that reboiler is heated, can cause temperature and the flowed fluctuation of reboiler steam that produce and that offer desorber, thereby cause the desorption technique of desorber unstable.

In addition, in the prior art, provide the gas that reclaims acid making system 40 to desorption gas to have flow and the irrational phenomenon of pressure, affect the direct motion of technique.

Summary of the invention

For prior art above shortcomings, one or more during one of object of the present invention is to address the above problem.

An aspect of of the present present invention provides a kind of control system for renewable flue gas desulfurization system, described control system comprises reboiler temperature control module and sulphur dioxide blower control module, wherein, described reboiler temperature control module comprises the first temperature element, the second temperature element, heat sink, flow adjusting valve for steam and the first control element, described the first temperature element is arranged on to be provided in the vapour source of thermal source for reboiler, described the second temperature element is arranged in the Steam area that will heat desulfuration solution lean solution in reboiler, described heat sink is arranged on the steam conveying pipe that connects vapour source and reboiler, described flow adjusting valve for steam is arranged on described steam conveying pipe, described the first control element is connected to receive respectively the temperature data from the first temperature element and the second temperature element with the second temperature element with the first temperature element, and respectively the described temperature data from the first temperature element or the second temperature element and process requirements temperature are compared, and described the first control element is also connected respectively to determine whether starting heat sink according to the result of described comparison with flow adjusting valve for steam with heat sink and/or flow adjusting valve for steam is lowered the temperature to steam, so that the temperature of steam approaches described process requirements temperature, described sulphur dioxide blower control module comprises flow measuring element, pressure measuring element, gas flow control valve and the second control element, described flow measuring element is arranged on the pipeline being connected with the air inlet of sulphur dioxide blower, described pressure measuring element is arranged on the pipeline that connects sulphur dioxide blower and sulphuric acid plant, described gas flow control valve is arranged on the pipeline between flow measuring element and the air inlet of sulphur dioxide blower, the second control element respectively with flow measuring element, pressure measuring element, the switch of gas flow control valve and sulphur dioxide blower is connected.

In one exemplary embodiment of the present invention, described the first control element can comprise the first data receiver unit, the first data processing unit and the first command unit, wherein, the first data receiver unit is connected with the second temperature element with the first temperature element respectively, for receiving the temperature data from the first temperature element and the second temperature element; The first data processing unit is connected between the first data receiver unit and the first command unit, for respectively the described temperature data from the first temperature element and the second temperature element and process requirements temperature being compared and comparative result is sent to the first command unit; The first command unit is connected with flow adjusting valve for steam with heat sink respectively; Described the second control element can comprise the second data receiver unit, the second data processing unit and the second command unit, wherein, the second data receiver unit is connected with pressure measuring element with flow measuring element respectively, for receiving from the data on flows of flow measuring element with from the pressure data of pressure measuring element; The second data processing unit is connected between the second data receiver unit and the second command unit, for respectively by described data on flows and target flow and by pressure data and goal pressure compares and comparative result is sent to the second command unit; The second command unit is connected with the switch of gas flow control valve and sulphur dioxide blower respectively.

In one exemplary embodiment of the present invention, described the first temperature element or the second temperature element can be thermal resistance or thermocouple, and described flow measuring element can be for being applicable to the flowmeter of etchant gas, and described pressure measuring element can be gas gauge.

In one exemplary embodiment of the present invention, described heat sink can comprise condensate liquid storage device and the condensate liquid spray thrower connecting by pipeline, and described condensate liquid spray thrower can be arranged in described steam conveying pipe and have the valve of adjustable condensate liquid flow.

In one exemplary embodiment of the present invention, described the first data processing unit can comprise the first look-up table, described the first look-up table stores has a plurality of the first values, the cooling degree of the heat sink that described the first value representation is corresponding with temperature from the first temperature element or the second temperature element and described process requirements temperature and/or the aperture of flow adjusting valve for steam; Described the second data processing unit can comprise second look-up table.Described second look-up table stores a plurality of the second values, the aperture of the gas flow control valve that the comparative result of described the second value representation and data on flows and target flow and pressure data and the comparative result of goal pressure are corresponding and/or the switch of sulphur dioxide blower.

It is a kind of according to the control method of above-mentioned control system that another aspect of the present invention provides.Described control method comprises without the reboiler temperature of sequencing controls step and sulphur dioxide blower is controlled step, and wherein, described reboiler temperature is controlled step and comprised: the temperature that is about to provide to steam in the vapour source of reboiler is provided; The temperature of steam in described vapour source and process requirements temperature are compared, when the temperature of steam is higher than described process requirements temperature in described vapour source, the steam in described vapour source is lowered the temperature; Measurement enters the temperature of the steam in reboiler after described cooling step; The temperature and the described process requirements temperature that after described cooling step, enter the steam in reboiler are compared, when entering the temperature of the steam in reboiler while being greater than described process requirements temperature after described cooling step, reduce will enter the flow of the steam in reboiler or increase the degree that the steam in described vapour source is lowered the temperature, so that the temperature of steam is close to described process requirements temperature; Described sulphur dioxide blower is controlled step and is comprised: measure and be about to enter the gas flow of sulphur dioxide blower and provide to the pressure of the gas of sulphuric acid plant from sulphur dioxide blower; Respectively by described gas flow and pressure and corresponding flow setting value and pressure set points comparison; According to the result of described comparison, control and enter the gas flow of sulphur dioxide blower and provide to the pressure of the gas of sulphuric acid plant from sulphur dioxide blower.

In one exemplary embodiment of the present invention, described reboiler can be connected with the desorber of renewable flue gas desulfurization system, take the heating liquid that flows into reboiler from desorber is steam, and the air inlet of described sulphur dioxide blower is connected with the sulfur dioxide outlet of drying tower, gas-liquid separator and desorber successively by pipeline.

In one exemplary embodiment of the present invention, described process requirements Temperature Setting is 115 ± 5 ℃.

In one exemplary embodiment of the present invention, described cooling step is realized by the steam spray condensate liquid in described vapour source.

In one exemplary embodiment of the present invention, the spray flux of described condensate liquid can calculate by conventional heat exchange efficiency.

Compared with prior art, beneficial effect of the present invention is the vapor (steam) temperature that enters reboiler to be controlled in the scope of technological requirement, thereby reduced reboiler incrustation, heat exchange efficiency and steam utilization have been improved, and can rationally control flow and the pressure of the gas that enters sulphur dioxide blower and sulphuric acid plant, guarantee the direct motion of acid-making process.In addition, control system of the present invention and method can also be stablized temperature and the flow of the steam that produce and that offer desorber from reboiler, have guaranteed the desorption technique stable smooth operation of desorber.

Accompanying drawing explanation

Fig. 1 shows the schematic diagram of the renewable flue gas desulfurization system that existing skill states

Fig. 2 shows according to an exemplary embodiment of the present invention the schematic diagram for the control system of renewable flue gas desulfurization system

Main Reference numeral comprises:

Reboiler 10, desorber 20, absorption tower 30, desorption gas reclaim acid making system 40, the first temperature element 11, the second temperature element 12, heat sink 13, flow adjusting valve for steam 14, the first control element 15, vapour source 16, gas-liquid separator 41, drying tower 42, sulphur dioxide blower 43, sulphuric acid plant 44, flow measuring element 51, pressure measuring element 52, gas flow control valve 53 and the second control element 54.

The specific embodiment

Hereinafter, in connection with accompanying drawing and exemplary embodiment, describe the control system for renewable flue gas desulfurization system of the present invention and control method in detail.By description below, will make spirit of the present invention and design more clearly convey to those skilled in the art.

Fig. 1 shows the schematic diagram of the renewable flue gas desulfurization system that existing skill states.

As shown in Figure 1, renewable flue gas desulfurization system generally includes reboiler 10, desorber 20, absorption tower 30 and desorption gas and reclaims acid making system 40.Wherein, 30 bottoms, absorption tower are connected to desorber 20, to provide desulfuration solution rich solution (that is, being rich in the desulfuration solution of oxysulfide) with the top of desorber 20 by pipeline; Desorption gas reclaims acid making system 40 and is arranged on the top of desorber 20 and is connected reclaim the high purity sulphur oxide gas (for example, sulfur dioxide and/or sulfur trioxide) in desorption gas and be made into the concentrated sulfuric acid with the desorption gas outlet of desorber 20; The bottom of desorber 20 is connected with reboiler 10; The bottom of desorber 20 is connected the desulfuration solution (that is, desulfuration solution lean solution) that completes desorb in desorber 20 to be sent into the top on absorption tower with the top on absorption tower by pipeline; From top, enter the desulfuration solution lean solution on absorption tower 30 and contact to absorb oxysulfide wherein with the flue gas adverse current that contains oxysulfide that enters absorption tower 30 from bottom, realize the purification to flue gas simultaneously, after counter current contacting, desulfuration solution lean solution becomes desulfuration solution rich solution.Specifically, in the desorption technique of renewable flue gas desulphurization process, the desulfuration solution rich solution obtaining from absorption technique can enter desorber 20 through spray thrower from desorber 20 tops, the high-temperature steam that reboiler 10 provides simultaneously enters desorber 20 from desorber 20 bottoms, described high-temperature steam and desulfuration solution rich solution carry out counter current contacting, so that desulfuration solution rich solution is heated, thus desulfuration solution rich solution desorption gas and desulfuration solution lean solution that in desorber 20, desorb contains high purity sulphur oxide with formation.Desulfuration solution lean solution enters reboiler 10 from desorber 20 bottoms, and the Steam Heating in the vapour source then being come from the outside in reboiler 10 and vaporizing forms steam, reenters desorber 20 subsequently carry out further desorb from reboiler 10 tops through pipeline.Here, described desulfuration solution rich solution refers to that absorption technique obtains contains oxysulfide (for example, SO 2) desulfuration solution; Described desulfuration solution lean solution refers in desorption technique has carried out to desulfuration solution rich solution the desulfuration solution obtaining after desorb at least one times.Obviously, the oxysulfide content in described desulfuration solution rich solution is higher than the oxysulfide content in described desulfuration solution lean solution.

Fig. 2 shows according to an exemplary embodiment of the present invention the schematic diagram for the control system of renewable flue gas desulfurization system.

As shown in Figure 2, in one exemplary embodiment of the present invention, for the control system of renewable flue gas desulfurization system, comprise reboiler temperature control module and sulphur dioxide blower control module.Wherein, reboiler temperature control module comprises the first temperature element 11, the second temperature element 12, heat sink 13, flow adjusting valve for steam 14 and the first control element 15; Sulphur dioxide blower control module comprises flow measuring element 51, pressure measuring element 52, gas flow control valve 53 and the second control element 54.Sulphur dioxide blower control module is arranged on sulphur dioxide blower 43 places that desorption gas reclaims acid making system 40.In this exemplary embodiment, desorption gas reclaims acid making system 40 and comprises in turn gas-liquid separator 41, drying tower 42, sulphur dioxide blower 43 and sulphuric acid plant 44.Gas phase and liquid phase the desorption gas that contains pure oxysulfide and steam that gas-liquid separator 41 can make to discharge from desorber 20 tops realize gas-liquid separation.Drying tower 42 is for the dry gas that contains oxysulfide obtaining from gas-liquid separator 41.Sulphur dioxide blower 43 is for providing the gas that contains oxysulfide through super-dry to sulphuric acid plant 44.In the present embodiment, sulphur dioxide blower 43 adopts cfentrifugal blower.Sulphuric acid plant 44 forms the concentrated sulfuric acid (concentrated sulfuric acid that for example, concentration is 98%) by the oxysulfide containing in gas.

The first temperature element 11 is arranged in the pipeline being connected with vapour source 16, for being about to provide to reboiler 10 and for reboiler 10 temperature of the steam of thermal source is provided from vapour source 16 is provided.The first temperature element 11 can be thermal resistance or thermocouple.In addition, the first temperature element 11 also can be arranged in vapour source 16, or is arranged on the steam conveying pipe between vapour source 16 and heat sink 13.

It is interior by the Steam area of heating desulfuration solution lean solution, for measuring the temperature that enters the steam in reboiler 10 from vapour source 16 that the second temperature element 12 is arranged on reboiler 10.The second temperature element 12 can be thermal resistance or thermocouple.

Heat sink 13 is arranged on the steam conveying pipe that connects vapour source 16 and reboiler 10, for to providing to the steam of reboiler 10 and lower the temperature through steam conveying pipe from vapour source 16.In addition, in another embodiment, heat sink 13 can comprise condensate liquid storage device (not shown) and the condensate liquid spray thrower (not shown) connecting by pipeline.Described condensate liquid storage device can be condensate drum, for storing condensate liquid.Described condensate liquid spray thrower is arranged in described steam conveying pipe and has the valve of adjustable condensate liquid flow, thereby can carry out in various degree cooling to the steam in steam conveying pipe.In one exemplary embodiment, the spray flux of described condensate liquid can calculate by conventional heat exchange efficiency.For example, those skilled in the art can be by the heat exchange efficiency to vapor (steam) temperature, the steam temperature in reboiler that enters reboiler steam temperature, process requirements, condensate liquid and steam in steam flow, vapour source, and vapor stream calculates and obtains the spray flux of condensate liquid through the parameters such as heat loss of steam conveying pipe.

Flow adjusting valve for steam 14 is arranged on to be stated on steam conveying pipe, for controlling the flow of the steam that enters reboiler 10.Although in Fig. 2, flow adjusting valve for steam 14 is arranged on the steam conveying pipe between vapour source 16 and heat sink 13, but the invention is not restricted to this, that is to say, flow adjusting valve for steam 14 also can be arranged on the conveyance conduit between reboiler 10 and heat sink 13.

The first control element 15 is connected with the second temperature element 12 with the first temperature element 11 respectively, to receive the temperature data from the first temperature element 11 and the second temperature element 12, and respectively the described temperature data from the first temperature element 11 or the second temperature element 12 and process requirements temperature are compared.The first control element 15 is also connected to determine whether starting heat sink according to the result of described comparison with flow adjusting valve for steam 14 with heat sink 13 respectively and/or flow adjusting valve for steam is lowered the temperature to steam, so that the temperature of steam approaches described process requirements temperature.

In addition,, in another exemplary embodiment, the first control element 15 can comprise the first data receiver unit (not shown) connected to one another, the first data processing unit (not shown) and the first command unit (not shown).Wherein, the first data receiver unit is connected with the second temperature element 12 with the first temperature element 11 respectively, for receiving the temperature data from the first temperature element 11 and the second temperature element 12; The first data processing unit is connected between the first data receiver unit and the first command unit, for respectively the described temperature data from the first temperature element 11 and the second temperature element 12 and process requirements temperature being compared and comparative result is sent to the first command unit; The first command unit is connected with flow adjusting valve for steam 14 with heat sink 13 respectively, to control the startup of heat sink 13 and the aperture of cooling degree and flow adjusting valve for steam 14 size thereof, so that the temperature of steam approaches described process requirements temperature.

In addition,, in another exemplary embodiment, for handled easily, the first data processing unit also can comprise the first look-up table.In the first look-up table, store many groups and control the value of the cooling degree of heat sink 13 and/or the aperture of flow adjusting valve for steam 14, described value is corresponding with temperature and described process requirements temperature from the first temperature element 11 or the second temperature element 12.Described the first look-up table can be two, and one for storing the value of the cooling degree of the heat sink 13 corresponding with the difference of temperature from the first temperature element 11 and described process requirements temperature; Another is for storing the value of the aperture of the flow adjusting valve for steam 14 corresponding with the difference of temperature from the second temperature element 12 and described process requirements temperature.Described the first look-up table can be by calculating and obtain through the parameters such as heat loss of steam conveying pipe heat exchange efficiency, the vapor stream of vapor (steam) temperature, the steam temperature in reboiler that enters reboiler steam temperature, process requirements, condensate liquid and steam in steam flow, condensate liquid flow, vapour source.In addition, described the first look-up table also can obtain by statistics rule, for example, and by then the reboiler temperature control module connecting according to the present invention is taken multiple measurements and averages and obtain.

Although described the example of the first control element 15 above, it will be apparent to those skilled in the art that and the invention is not restricted to this.For example, the first control element 15 in control system of the present invention can be a PLC controller or thermostatical automatic control device, described PLC controller or thermostatical automatic control device can receive the temperature data from the first temperature element 11 and the second temperature element 12, and by described, from temperature data and the process requirements temperature of the first temperature element 11 and the second temperature element 12, do not compare respectively, then according to comparative result, respectively heat sink 13 and flow adjusting valve for steam 14 are controlled.

Although described some exemplary embodiments of control system of the present invention above, should be clear but this area skill is stated personnel, control system of the present invention is for example not limited to above-described embodiment, and control system of the present invention also can be by integrating to realize by two or three in the first control element 15, heat sink 13, the first temperature element 11, the second temperature element 12 and flow adjusting valve for steam 14 are above.

Flow measuring element 51 is arranged on the pipeline being connected with the carrying out mouth of sulphur dioxide blower 43, for measuring the flow from the gas of drying tower 42.Here, flow measuring element 51 can be the flowmeter that is applicable to etchant gas.

Pressure measuring element 52 is arranged on the pipeline that connects sulphur dioxide blower 43 and sulphuric acid plant 44, for measuring the pressure of the gas that is about to offer sulphuric acid plant 44.Here, pressure measuring element 52 can be gas gauge.

Gas flow control valve 53 is arranged on the pipeline between flow measuring element 51 and the air inlet of sulphur dioxide blower 43, for adjusting the amount of the gas that enters sulphur dioxide blower 43.

The second control element 54 respectively with flow measuring element 51, pressure measuring element 52, the switch 55 of gas flow control valve 53 and sulphur dioxide blower is connected.Here, the switch 55 of sulphur dioxide blower is for regulating the operation frequency of sulphur dioxide blower, the pressure data that the data on flows that the second control element 54 can record flow measuring element 51 and pressure measuring element 52 record compares with providing to the predetermined atmospheric pressure value of sulphuric acid plant 44 of the predetermined flow value of the gas that enters sulphur dioxide blower 43 of technological requirement and technological requirement respectively, and according to comparative result, control the aperture of the aperture of gas flow control valve 53 and the switch of sulphur dioxide blower 55.Gas flow control valve 53 can be triple valve, thereby when gas flow is greater than the predetermined flow value of technological requirement, by a part of gas distribution.The switch 55 of sulphur dioxide blower can be adjusted the power of sulphur dioxide blower, thereby can adjust the pressure of the gas that enters sulphuric acid plant 44.

In addition,, in another exemplary embodiment, the second control element can comprise the second data receiver unit (not shown), the second data processing unit (not shown) and the second command unit (not shown).Wherein, the second data receiver unit is connected with pressure measuring element 52 with flow measuring element 51 respectively, for receiving from the data on flows of flow measuring element 51 with from the pressure data of pressure measuring element 52; The second data processing unit is connected between the second data receiver unit and the second command unit, for example, for respectively by described data on flows and target flow (, the predetermined flow value of the gas that enters sulphur dioxide blower 43 of technological requirement) and by pressure data and goal pressure (for example, technological requirement the predetermined atmospheric pressure value to sulphuric acid plant 44 is provided) compare, and comparative result is sent to the second command unit; The second command unit is connected with the switch 55 of gas flow control valve 53 and sulphur dioxide blower respectively, the control realizing the flow of gas and/or pressure with the switch 55 by adjusting gas flow control valve 53 and/or sulphur dioxide blower, thus make the flow of gas and/or pressure meet technological requirement.

In addition,, in another exemplary embodiment, for handled easily, the second data processing unit also can comprise second look-up table.The value that stores the aperture of the many groups of switches that can control gas flow control valve and/or sulphur dioxide blower in second look-up table, described value is corresponding with the comparative result of goal pressure with comparative result and the pressure data of data on flows and target flow.Described second look-up table can be two, and one for storing the value of the aperture of the gas flow control valve corresponding with the comparative result of data on flows and target flow 53; Another is for storing the value of aperture of the switch 55 of the sulphur dioxide blower corresponding with pressure data and the comparative result of goal pressure.Described second look-up table can be by obtaining the calculating of the flow value of gas flow, pressure and technological requirement and force value.In addition, described second look-up table also can obtain by statistics rule, for example, and by then the sulphur dioxide blower control module connecting according to the present invention is taken multiple measurements and averages and obtain.

Although described the example of the second control element 54 above, it will be apparent to those skilled in the art that and the invention is not restricted to this.For example, the second control element 15 in control system of the present invention can be the automaton of a PLC controller or gas pressure and flow.

The method of controlling according to an exemplary embodiment of the present invention renewable flue gas desulfurization system can comprise without sequencing to the control of reboiler temperature and the control to sulphur dioxide blower.

Particularly.To the control of reboiler temperature, can comprise the following steps:

(1) measure and to be about to provide to reboiler and to heat the temperature of steam in the vapour source of desulfuration solution lean solution.This step can realize by the first temperature element 11.

(2) set the process requirements temperature that enters the steam in reboiler.Described process requirements temperature can be set as the temperature value or the temperature range that meet technological requirement and seldom in reboiler, produce incrustation.For example, in the present embodiment, described process requirements temperature can be set as 115 ± 5 ℃.

(3) temperature of steam in described vapour source and described process requirements temperature are compared, when the temperature of steam is higher than described process requirements temperature in described vapour source, the steam in described vapour source is lowered the temperature.This step can realize by the first control element 15 and heat sink 13.

(4) measure and after described cooling step, enter the temperature of the steam in reboiler.This step can realize by the second temperature element 12.

(5) temperature and the described process requirements temperature that after described cooling step, enter the steam in reboiler are compared, when entering the temperature of the steam in reboiler while being greater than described process requirements temperature after described cooling step, reduce to enter the flow of the steam in reboiler or increase the degree that the steam in described vapour source is lowered the temperature.This step can realize by the first control element 15, heat sink 13 and flow adjusting valve for steam 14.Here, the first control element 15 can repeatedly be adjusted heat sink 13 and/or flow adjusting valve for steam 14 according to the comparative result of temperature, for example, until enter the requirement (, equal or approach described process requirements temperature) that the vapor (steam) temperature of reboiler meets described process requirements temperature.

To the control of sulphur dioxide blower, can comprise the following steps:

(1) measure and be about to enter the gas flow of sulphur dioxide blower and provide to the pressure of the gas of sulphuric acid plant from sulphur dioxide blower.This step can realize by flow measuring element 51 and pressure measuring element 53.

(2) respectively by described gas flow and pressure and corresponding flow setting value and pressure set points comparison.Here, flow setting value can be the predetermined flow value of the gas that enters sulphur dioxide blower 43 of technological requirement, and pressure set points can be the predetermined atmospheric pressure value to sulphuric acid plant 44 that provides of technological requirement.

(3) according to the result of described comparison, control and enter the gas flow of sulphur dioxide blower and provide to the pressure of the gas of sulphuric acid plant from sulphur dioxide blower.This step can realize by switch 55 and the gas flow control valve 53 of the second control element 54, sulphur dioxide blower.The second control element 54 receives flow measuring element 51 and/or the real-time measuring flow data of pressure measuring element 52 and/or pressure data, then measured real time data and target data compare, if real time data is greater than corresponding target data, control switch 55 and the gas flow control valve 53 of sulphur dioxide blower, so that the flow of gas and/or pressure are adjusted, until approach target data.Here, the second control element can repeatedly be adjusted data on flows and/or pressure data, until the flow of gas and/or pressure approach or equals corresponding target data.

In sum, according to the control system for renewable flue gas desulfurization system of the present invention and method, the vapor (steam) temperature that enters reboiler can be controlled in the scope of technological requirement, thereby reduced reboiler incrustation, heat exchange efficiency and steam utilization have been improved, and can rationally control flow and the pressure of the gas that enters sulphur dioxide blower and sulphuric acid plant, guarantee the direct motion of acid-making process.In addition, control system of the present invention and method can also be stablized temperature and the flow of the steam that produce and that offer desorber from reboiler, have guaranteed the desorption technique stable smooth operation of desorber.

Although described the present invention in conjunction with some exemplary embodiments above, it will be apparent to those skilled in the art that in the situation that do not depart from the spirit and scope that claim limits, can above-mentioned exemplary embodiment be modified and be changed.

Claims (10)

1. for a control system for renewable flue gas desulfurization system, it is characterized in that, described control system comprises reboiler temperature control module and sulphur dioxide blower control module, wherein,
Described reboiler temperature control module comprises the first temperature element, the second temperature element, heat sink, flow adjusting valve for steam and the first control element, described the first temperature element is arranged on to be provided in the vapour source of thermal source for reboiler, described the second temperature element is arranged in the Steam area that will heat desulfuration solution lean solution in reboiler, described heat sink is arranged on the steam conveying pipe that connects vapour source and reboiler, described flow adjusting valve for steam is arranged on described steam conveying pipe, described the first control element is connected to receive respectively the temperature data from the first temperature element and the second temperature element with the second temperature element with the first temperature element, and respectively the described temperature data from the first temperature element or the second temperature element and process requirements temperature are compared, and described the first control element is also connected respectively to determine whether starting heat sink according to the result of described comparison with flow adjusting valve for steam with heat sink and/or flow adjusting valve for steam is lowered the temperature to steam, so that the temperature of steam approaches described process requirements temperature,
Described sulphur dioxide blower control module comprises flow measuring element, pressure measuring element, gas flow control valve and the second control element, described flow measuring element is arranged on the pipeline being connected with the air inlet of sulphur dioxide blower, described pressure measuring element is arranged on the pipeline that connects sulphur dioxide blower and sulphuric acid plant, described gas flow control valve is arranged on the pipeline between flow measuring element and the air inlet of sulphur dioxide blower, the second control element respectively with flow measuring element, pressure measuring element, the switch of gas flow control valve and sulphur dioxide blower is connected.
2. the control system for renewable flue gas desulfurization system according to claim 1, is characterized in that,
Described the first control element comprises the first data receiver unit, the first data processing unit and the first command unit, wherein, the first data receiver unit is connected with the second temperature element with the first temperature element respectively, for receiving the temperature data from the first temperature element and the second temperature element; The first data processing unit is connected between the first data receiver unit and the first command unit, for respectively the described temperature data from the first temperature element and the second temperature element and process requirements temperature being compared and comparative result is sent to the first command unit; The first command unit is connected with flow adjusting valve for steam with heat sink respectively;
Described the second control element comprises the second data receiver unit, the second data processing unit and the second command unit, wherein, the second data receiver unit is connected with pressure measuring element with flow measuring element respectively, for receiving from the data on flows of flow measuring element with from the pressure data of pressure measuring element; The second data processing unit is connected between the second data receiver unit and the second command unit, for respectively by described data on flows and target flow and by pressure data and goal pressure compares and comparative result is sent to the second command unit; The second command unit is connected with the switch of gas flow control valve and sulphur dioxide blower respectively.
3. the control system for renewable flue gas desulfurization system according to claim 1 and 2, it is characterized in that, described the first temperature element or the second temperature element are thermal resistance or thermocouple, described flow measuring element is the flowmeter that is applicable to etchant gas, and described pressure measuring element is gas gauge.
4. the control system for renewable flue gas desulfurization system according to claim 1 and 2, it is characterized in that, described heat sink comprises condensate liquid storage device and the condensate liquid spray thrower connecting by pipeline, and described condensate liquid spray thrower is arranged in described steam conveying pipe and has the valve of adjustable condensate liquid flow.
5. the control system for renewable flue gas desulfurization system according to claim 2, it is characterized in that, described the first data processing unit comprises the first look-up table, described the first look-up table stores has a plurality of the first values, the cooling degree of the heat sink that described the first value representation is corresponding with temperature from the first temperature element or the second temperature element and described process requirements temperature and/or the aperture of flow adjusting valve for steam; Described the second data processing unit comprises second look-up table, described second look-up table stores a plurality of the second values, the aperture of the gas flow control valve that the comparative result of described the second value representation and data on flows and target flow and pressure data and the comparative result of goal pressure are corresponding and/or the switch of sulphur dioxide blower.
6. a control method for control system according to claim 1, is characterized in that, described control method comprises without the reboiler temperature of sequencing controls step and sulphur dioxide blower control step, wherein,
Described reboiler temperature is controlled step and is comprised: the temperature that is about to provide to steam in the vapour source of reboiler is provided; The temperature of steam in described vapour source and process requirements temperature are compared, when the temperature of steam is higher than described process requirements temperature in described vapour source, the steam in described vapour source is lowered the temperature; Measurement enters the temperature of the steam in reboiler after described cooling step; The temperature and the described process requirements temperature that after described cooling step, enter the steam in reboiler are compared, when entering the temperature of the steam in reboiler while being greater than described process requirements temperature after described cooling step, reduce will enter the flow of the steam in reboiler or increase the degree that the steam in described vapour source is lowered the temperature, so that the temperature of steam is close to described process requirements temperature;
Described sulphur dioxide blower is controlled step and is comprised: measure and be about to enter the gas flow of sulphur dioxide blower and provide to the pressure of the gas of sulphuric acid plant from sulphur dioxide blower; Respectively by described gas flow and pressure and corresponding flow setting value and pressure set points comparison; According to the result of described comparison, control and enter the gas flow of sulphur dioxide blower and provide to the pressure of the gas of sulphuric acid plant from sulphur dioxide blower.
7. control method according to claim 6, it is characterized in that, described reboiler is connected with the desorber of renewable flue gas desulfurization system, take the heating liquid that flows into reboiler from desorber is steam, and the air inlet of described sulphur dioxide blower is connected with the sulfur dioxide outlet of drying tower, gas-liquid separator and desorber successively by pipeline.
8. control method according to claim 6, is characterized in that, described process requirements Temperature Setting is 115 ± 5 ℃.
9. control method according to claim 6, is characterized in that, described cooling step is realized by the steam spray condensate liquid in described vapour source.
10. control method according to claim 9, is characterized in that, the spray flux of described condensate liquid can calculate by conventional heat exchange efficiency.
CN201110416707.7A 2011-12-14 2011-12-14 Control system for renewable flue gas desulfurization system and control method CN102512917B (en)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101357294A (en) * 2007-08-04 2009-02-04 山东省冶金设计院有限责任公司 Renewable devulcanizing technological process and use thereof
CN101703880A (en) * 2009-11-02 2010-05-12 西安交通大学 Power plant flue gas desulphurization and decarbonization integrated purification system
CN101708414A (en) * 2009-12-31 2010-05-19 攀钢集团研究院有限公司 System and method for desulphurizing waste gas by cyclic absorption and application thereof

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0355171B2 (en) * 1983-03-15 1991-08-22

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101357294A (en) * 2007-08-04 2009-02-04 山东省冶金设计院有限责任公司 Renewable devulcanizing technological process and use thereof
CN101703880A (en) * 2009-11-02 2010-05-12 西安交通大学 Power plant flue gas desulphurization and decarbonization integrated purification system
CN101708414A (en) * 2009-12-31 2010-05-19 攀钢集团研究院有限公司 System and method for desulphurizing waste gas by cyclic absorption and application thereof

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