CN102512917A - 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 PDFInfo
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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
Technical field
The present invention relates to the automatic control technology field, more particularly, relate to a kind of control system and control method that is used for renewable flue gas desulphurization system.
Background technology
Reboiler (also claiming reboiler) is the device that liquid is vaporized again through heating.Said heating can realize from the steam of vapour source through inserting to reboiler.In other words, reboiler be one can heat-shift, have the special heat exchanger of vaporization space simultaneously.
Renewable flue gas desulphurization system is the device that is used to implement renewable flue gas desulfurization technique.Fig. 1 shows the sketch map of the renewable flue gas desulphurization system of prior art.As shown in Figure 1, renewable flue gas desulphurization system generally includes reboiler 10, desorber 20, absorption tower 30 and desorption gas and reclaims acid making system 40.Usually; Said renewable flue gas desulfurization technique can may further comprise the steps: at first; In absorption tower 30; The desulfuration solution of utilization such as amine liquid or ionic liquid absorb in the flue gas (comprising various flue gases that contain oxysulfide or industrial waste gas, for example, sintered discharge gas, blast furnace gas, coke-stove gas, coal-fired plant boiler waste gas, heating furnace waste gas etc.) such as the oxysulfide gas of sulfur dioxide and sulfur trioxide and realize purification to flue gas; Then; In desorber 20; Oxysulfide gas in the liquation of desorb desulfurization at high temperature obtaining highly purified oxysulfide gas, and is restored simultaneously and absorbs the desulfuration solution of oxysulfide gas ability; Desulfuration solution after the desorb is provided to the absorption tower again and absorbs the oxysulfide gas in the flue gas, thereby realizes the circulation of absorption step and desorption procedure.
Reboiler can be connected with the desorber 20 of renewable flue gas desulphurization system, will being heated to be steam from the liquid (for example, containing the desulfuration solution of oxysulfide) that desorber 20 flows into reboilers, thereby promotes the desorb of said liquid in desorber.
Yet, in the prior art, owing to the vapor (steam) temperature of the vapour source that is used for reboiler is heated is higher usually; So cause reboiler incrustation serious; And then cause heat exchange efficiency to reduce and waste of steam, and even will cause reboiler to stop up when serious, thus normally carrying out of producing of influence.
In addition,, then can cause the temperature and the flowed fluctuation of reboiler steam that produce and that offer desorber, thereby cause the desorption technique of desorber unstable if there is large-scale temperature fluctuation in the high-temperature steam of the vapour source that is used for reboiler is heated.
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, influence the direct motion of technology.
Summary of the invention
The above-mentioned deficiency that exists to prior art, one or more during one of the object of the invention is to address the above problem.
One side of the present invention provides a kind of control system that is used for renewable flue gas desulphurization system; Said control system comprises reboiler temperature control module and sulfur dioxide air blast control module; Wherein, Said reboiler temperature control module comprises first temperature element, second temperature element, heat sink, steam flow control valve and first control element; Said first temperature element is arranged on to reboiler and provides in the vapour source of thermal source; Said second temperature element is arranged in the Steam area that will heat the desulfuration solution lean solution in the reboiler; Said heat sink is arranged on the steam conveying pipe that connects vapour source and reboiler; Said steam flow control valve is arranged on the said steam conveying pipe, and said first control element is connected with second temperature element with the temperature data of reception from first temperature element and second temperature element with first temperature element respectively, and respectively said temperature data and process requirements temperature from first temperature element or second temperature element is compared; And said first control element also is connected with the steam flow control valve with the result according to said comparison with heat sink respectively and determines whether starting heat sink and/or the steam flow control valve comes steam is lowered the temperature, so that the temperature of steam is near said process requirements temperature; Said sulfur dioxide air blast control module comprises flow measuring element, pressure measuring element, gas flow control valve and second control element; Said flow measuring element is arranged on the pipeline that is connected with the air inlet of sulfur dioxide air blast; Said pressure measuring element is arranged on the pipeline that connects sulfur dioxide air blast and sulphuric acid plant; Said gas flow control valve is arranged on the pipeline between the air inlet of flow measuring element and sulfur dioxide air blast, and second control element is connected with flow measuring element, pressure measuring element, gas flow control valve and the switch of sulfur dioxide air blast respectively.
In one exemplary embodiment of the present invention; Said first control element can comprise the first data receiving element, first data processing unit and first command unit; Wherein, The first data receiving element is connected with second temperature element with first temperature element respectively, to be used to receive the temperature data from first temperature element and second temperature element; First data processing unit is connected between the first data receiving element and first command unit, said temperature data and process requirements temperature from first temperature element and second temperature element is compared and comparative result is sent to first command unit being used for respectively; First command unit is connected with the steam flow control valve with heat sink respectively; Said second control element can comprise the second data receiving element, second data processing unit and second command unit; Wherein, The second data receiving element is connected with pressure measuring element with flow measuring element respectively, to be used to receive from the data on flows of flow measuring element with from the pressure data of pressure measuring element; Second data processing unit is connected between the second data receiving element and second command unit, to be used for respectively with said data on flows and target flow and with pressure data and goal pressure compares and comparative result is sent to second command unit; Second command unit is connected with the switch of gas flow control valve with the sulfur dioxide air blast respectively.
In one exemplary embodiment of the present invention, said first temperature element or second temperature element can be thermal resistance or thermocouple, and said flow measuring element can be for being applicable to the flowmeter of etchant gas, and said pressure measuring element can be gas gauge.
In one exemplary embodiment of the present invention; Said heat sink can comprise condensate liquid storage device and the condensate liquid spray thrower that connects through pipeline, and said condensate liquid spray thrower can be arranged in the said steam conveying pipe and have the valve of scalable condensate liquid flow.
In one exemplary embodiment of the present invention; Said first data processing unit can comprise first look-up table; Said first look-up table stores has a plurality of first values, said first value representation with from the cooling degree of the corresponding heat sink of the temperature of first temperature element or second temperature element and said process requirements temperature and/or the aperture of steam flow control valve; Said second data processing unit can comprise second look-up table.Said second look-up table stores a plurality of second values, the aperture of the gas flow control valve that the comparative result of said 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 sulfur dioxide air blast.
Another aspect of the present invention provides a kind of control method according to above-mentioned control system.Said control method comprises the reboiler temperature control step and sulfur dioxide air blast control step of no sequencing, and wherein, said reboiler temperature control step comprises: measurement is about to provide the temperature of steam to the vapour source of reboiler; The temperature and the process requirements temperature of steam in the said vapour source are compared, when the temperature of steam in the said vapour source is higher than said process requirements temperature, the steam in the said vapour source is lowered the temperature; Measurement gets into the temperature of the steam in the reboiler behind said cooling step; The temperature and the said process requirements temperature that will behind said cooling step, get into the steam in the reboiler compare; The temperature of the steam in behind said cooling step, getting into reboiler is during greater than said process requirements temperature; Reduce to get into the flow of the steam in the reboiler or increase the degree that the steam in the said vapour source is lowered the temperature, so that the temperature of steam approaches said process requirements temperature; Said sulfur dioxide air blast control step comprises: measurement is about to get into the gas flow of sulfur dioxide air blast and provides to the pressure of the gas of sulphuric acid plant from the sulfur dioxide air blast; Respectively said gas flow and pressure are compared with corresponding flow setting value and pressure set points; Control the gas flow that gets into the sulfur dioxide air blast and provide to the pressure of the gas of sulphuric acid plant according to the result of said comparison from the sulfur dioxide air blast.
In one exemplary embodiment of the present invention; Said reboiler can be connected with the desorber of renewable flue gas desulphurization system; Liquid heat will from desorber, flow into reboiler is a steam, and the air inlet of said sulfur dioxide air blast is connected with the sulfur dioxide outlet of drying tower, gas-liquid separator and desorber through pipeline successively.
In one exemplary embodiment of the present invention, said process requirements temperature is set at 115 ± 5 ℃.
In one exemplary embodiment of the present invention, said cooling step is realized through the steam spray cooling lime set in said vapour source.
In one exemplary embodiment of the present invention, the spray flux of said condensate liquid can calculate through the heat exchange efficiency of routine.
Compared with prior art; Beneficial effect of the present invention is and can the vapor (steam) temperature that get into reboiler be controlled in the scope of technological requirement; Thereby reduced reboiler incrustation; Improve heat exchange efficiency and steam utilization, and can rationally control the flow and the pressure of the gas that gets into sulfur dioxide air blast and sulphuric acid plant, guaranteed the direct motion of acid-making process.In addition, control system and method for the present invention can also be stablized from the temperature and the flow of reboiler steam that produce and that offer desorber, has guaranteed the desorption technique stable smooth operation of desorber.
Description of drawings
Fig. 1 shows the sketch map of the renewable flue gas desulphurization system that existing skill states
Fig. 2 shows the sketch map of the control system that is used for renewable flue gas desulphurization system according to an exemplary embodiment of the present invention
Main Reference numeral comprises:
The specific embodiment
Hereinafter, with combining accompanying drawing and exemplary embodiment to describe control system and the control method that is used for renewable flue gas desulphurization system of the present invention in detail.Through following description, will make spirit of the present invention and design more clearly convey to those skilled in the art.
Fig. 1 shows the sketch map of the renewable flue gas desulphurization system that existing skill states.
As shown in Figure 1, renewable flue gas desulphurization 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 so that desulfuration solution rich solution (that is, being rich in the desulfuration solution of oxysulfide) to be provided to desorber 20 through pipeline with the top of desorber 20; Desorption gas recovery acid making system 40 is arranged on the top of desorber 20 and is connected to reclaim the high purity sulphur oxide gas (for example, sulfur dioxide and/or sulfur trioxide) in the desorption gas and to 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 top of sending into the absorption tower with the desulfuration solution (that is desulfuration solution lean solution) that will in desorber 20, accomplish desorb with the top on absorption tower through pipeline; Get into the desulfuration solution lean solution on absorption tower 30 contacts to absorb oxysulfide wherein with the flue gas adverse current that contains oxysulfide that gets into absorption tower 30 from the bottom from top; Realize purification simultaneously to flue gas; After counter current contacting, the desulfuration solution lean solution becomes the desulfuration solution rich solution.Specifically; In the desorption technique of renewable flue gas desulfurization technique; The desulfuration solution rich solution that obtains from absorption technique can get into desorber 20 from desorber 20 tops through spray thrower; The high-temperature steam that while reboiler 10 provides gets into desorber 20 from desorber 20 bottoms; Said high-temperature steam and desulfuration solution rich solution carry out counter current contacting, and with desulfuration solution rich solution heating, thereby the desorb in desorber 20 of desulfuration solution rich solution contains the desorption gas and the desulfuration solution lean solution of high purity sulphur oxide with formation.The desulfuration solution lean solution gets into reboiler 10 from desorber 20 bottoms, in reboiler 10, vaporized by the Steam Heating in the vapour source that comes from the outside then, forms steam, gets into desorber 20 from reboiler 10 tops again through pipeline subsequently and carries out further desorb.Here, said desulfuration solution rich solution is meant that absorption technique obtains contains oxysulfide (for example, SO
2) desulfuration solution; Said desulfuration solution lean solution is meant in desorption technique has carried out the desulfuration solution that obtains after at least desorb to the desulfuration solution rich solution.Obviously, the oxysulfide content in the said desulfuration solution rich solution is higher than the oxysulfide content in the said desulfuration solution lean solution.
Fig. 2 shows the sketch map of the control system that is used for renewable flue gas desulphurization system according to an exemplary embodiment of the present invention.
As shown in Figure 2, in one exemplary embodiment of the present invention, the control system that is used for renewable flue gas desulphurization system comprises reboiler temperature control module and sulfur dioxide air blast control module.Wherein, the reboiler temperature control module comprises first temperature element 11, second temperature element 12, heat sink 13, steam flow control valve 14 and first control element 15; Sulfur dioxide air blast control module comprises flow measuring element 51, pressure measuring element 52, gas flow control valve 53 and second control element 54.Sulfur dioxide air blast control module is arranged on sulfur dioxide air blast 43 places that desorption gas reclaims acid making system 40.In this exemplary embodiment, desorption gas reclaims acid making system 40 and comprises gas-liquid separator 41 in order, drying tower 42, sulfur dioxide air blast 43 and sulphuric acid plant 44.Gas-liquid separator 41 can make gas phase and the liquid phase from the desorption gas that contains pure oxysulfide and steam that discharge on desorber 20 tops realize gas-liquid separation.Drying tower 42 is used for the dry gas that contains oxysulfide that obtains from gas-liquid separator 41.Sulfur dioxide air blast 43 is used for the gas that contains oxysulfide through super-dry is provided to sulphuric acid plant 44.In the present embodiment, sulfur dioxide air blast 43 adopts cfentrifugal blower.Sulphuric acid plant 44 forms the concentrated sulfuric acid (for example, concentration is 98% the concentrated sulfuric acid) with the oxysulfide that contains in the gas.
Heat sink 13 is arranged on the steam conveying pipe that connects vapour source 16 and reboiler 10, is used for lowering the temperature to providing to the steam of reboiler 10 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) that connects through pipeline.Said condensate liquid storage device can be condensate drum, is used to store condensate liquid.Said condensate liquid spray thrower is arranged in the said steam conveying pipe and has the valve of scalable condensate liquid flow, thereby can carry out cooling in various degree to the steam in the steam conveying pipe.In one exemplary embodiment, the spray flux of said condensate liquid can calculate through the heat exchange efficiency of routine.For example; Those skilled in the art can through to vapor (steam) temperature in steam flow, the vapour source, get into the heat exchange efficiency of vapor (steam) temperature, condensate liquid and steam in the reboiler of reboiler steam temperature, process requirements, vapor stream calculates and obtains the spray flux of condensate liquid through the parameters such as heat loss of steam conveying pipe.
Steam flow control valve 14 is arranged on to be stated on the steam conveying pipe, is used to control the flow of the steam that gets into reboiler 10.Although in Fig. 2; Steam flow control valve 14 is arranged on the steam conveying pipe between vapour source 16 and the heat sink 13; But the invention is not restricted to this, that is to say, steam flow control valve 14 also can be arranged on the conveyance conduit between reboiler 10 and the heat sink 13.
In addition, in another exemplary embodiment, first control element 15 can comprise the first data receiving element (not shown) connected to one another, the first data processing unit (not shown) and the first command unit (not shown).Wherein, the first data receiving element is connected with second temperature element 12 with first temperature element 11 respectively, to be used to receive the temperature data from first temperature element 11 and second temperature element 12; First data processing unit is connected between the first data receiving element and first command unit, said temperature data and process requirements temperature from first temperature element 11 and second temperature element 12 is compared and comparative result is sent to first command unit being used for respectively; First command unit is connected with steam flow control valve 14 with heat sink 13 respectively, with the startup of control heat sink 13 and the aperture size of cooling degree and steam flow control valve 14 thereof, so that the temperature of steam is near said process requirements temperature.
In addition, in another exemplary embodiment, operation for ease, first data processing unit also can comprise first look-up table.The value of the cooling degree of the control of group more than storing in first look-up table heat sinks 13 and/or the aperture of steam flow control valve 14, said value is corresponding with temperature and said process requirements temperature from first temperature element 11 or second temperature element 12.Said first look-up table can be two, and one is used to store and value from the cooling degree of the corresponding heat sink 13 of the difference of the temperature of first temperature element 11 and said process requirements temperature; Another is used to store and value from the aperture of the corresponding steam flow control valve 14 of the difference of the temperature of second temperature element 12 and said process requirements temperature.Said first look-up table can calculate through the parameters such as heat loss of steam conveying pipe and obtain through heat exchange efficiency, the vapor stream to vapor (steam) temperature, condensate liquid and steam in the reboiler of vapor (steam) temperature, entering reboiler steam temperature, process requirements in steam flow, condensate liquid flow, the vapour source.In addition, said first look-up table also can obtain through the statistics rule, for example, obtains through the reboiler temperature control module that connects according to the present invention is taken multiple measurements to average then.
Although described the example of first control element 15 above, it will be apparent to those skilled in the art that to the invention is not restricted to this.For example; First control element 15 in the control of the present invention system can be a PLC controller or thermostatical automatic control device; Said PLC controller or thermostatical automatic control device can receive the temperature data from first temperature element 11 and second temperature element 12; And do not compare from the temperature data and the process requirements temperature of first temperature element 11 and second temperature element 12 said respectively, respectively heat sink 13 and steam flow control valve 14 are controlled according to comparative result then.
Although described the certain exemplary embodiment of control of the present invention system above; Should be clear but this area skill is stated personnel; Control of the present invention system for example is not limited to the foregoing description, and control of the present invention system also can be through realizing integrating more than two or three in first control element 15, heat sink 13, first temperature element 11, second temperature element 12 and the steam flow control valve 14.
Gas flow control valve 53 is arranged on the pipeline between the air inlet of flow measuring element 51 and sulfur dioxide air blast 43, is used to adjust the amount of the gas that gets into sulfur dioxide air blast 43.
In addition, in another exemplary embodiment, second control element can comprise the second data receiving element (not shown), the second data processing unit (not shown) and the second command unit (not shown).Wherein, the second data receiving element is connected with pressure measuring element 52 with flow measuring element 51 respectively, to be used to receive from the data on flows of flow measuring element 51 with from the pressure data of pressure measuring element 52; Second data processing unit is connected between the second data receiving element and second command unit; (for example to be used for respectively with said data on flows and target flow; The predetermined flow value of the gas of the entering sulfur dioxide air blast 43 of technological requirement) and (for example with pressure data and goal pressure; Technological requirement the predetermined atmospheric pressure value to sulphuric acid plant 44 is provided) compare, and comparative result is sent to second command unit; Second command unit is connected with the switch 55 of gas flow control valve 53 and sulfur dioxide air blast respectively; With the control that realizes the flow and/or the pressure of gas through the switch 55 of adjustments of gas flow control valve 53 and/or sulfur dioxide air blast, thereby make the flow of gas and/or pressure satisfy technological requirement.
In addition, in another exemplary embodiment, operation for ease, second data processing unit also can comprise second look-up table.Store the value of the aperture of the many groups of switches that can control gas flow control valve and/or sulfur dioxide air blast in the second look-up table, said value is corresponding with the comparative result of goal pressure with the comparative result and the pressure data of data on flows and target flow.Said second look-up table can be two, a value that is used to store the aperture of the gas flow control valve corresponding with the comparative result of data on flows and target flow 53; Another is used to store the value of aperture of the switch 55 of the sulfur dioxide air blast corresponding with the pressure data and the comparative result of goal pressure.Said second look-up table can be through obtaining the flow value of gas flow, pressure and technological requirement and the calculating of force value.In addition, said second look-up table also can obtain through the statistics rule, for example, obtains through the sulfur dioxide air blast control module that connects according to the present invention is taken multiple measurements to average then.
Although described the example of second control element 54 above, it will be apparent to those skilled in the art that to the invention is not restricted to this.For example, second control element 15 in the control of the present invention system can be the automaton of a PLC controller or gas pressure and flow.
The method of controlling renewable flue gas desulphurization system according to an exemplary embodiment of the present invention can comprise no sequencing to the control of reboiler temperature with to the control of sulfur dioxide air blast.
Particularly.Control to reboiler temperature can may further comprise the steps:
(1) measures 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 through first temperature element 11.
(2) set the process requirements temperature that gets into the steam in the reboiler.Said process requirements temperature can be set at temperature value or the temperature range that satisfies technological requirement and seldom in reboiler, produce incrustation.For example, in the present embodiment, said process requirements temperature can be set at 115 ± 5 ℃.
(3) temperature and the said process requirements temperature with steam in the said vapour source compares, and when the temperature of steam in the said vapour source is higher than said process requirements temperature, the steam in the said vapour source lowered the temperature.This step can realize with heat sink 13 through first control element 15.
(4) measure the temperature that behind said cooling step, gets into the steam in the reboiler.This step can realize through second temperature element 12.
The temperature and the said process requirements temperature that (5) will behind said cooling step, get into the steam in the reboiler compare; The temperature of the steam in behind said cooling step, getting into reboiler reduces to get into the flow of the steam in the reboiler or increases the degree that the steam in the said vapour source is lowered the temperature during greater than said process requirements temperature.This step can realize through first control element 15, heat sink 13 and steam flow control valve 14.Here; First control element 15 can repeatedly be adjusted heat sink 13 and/or steam flow control valve 14 according to the comparative result of temperature; Satisfy the requirement (for example, equal or near said process requirements temperature) of said process requirements temperature until the vapor (steam) temperature that gets into reboiler.
Control to the sulfur dioxide air blast can may further comprise the steps:
(1) measurement is about to get into the gas flow of sulfur dioxide air blast and provides to the pressure of the gas of sulphuric acid plant from the sulfur dioxide air blast.This step can realize through flow measuring element 51 and pressure measuring element 53.
(2) respectively said gas flow and pressure are compared with corresponding flow setting value and pressure set points.Here, flow setting value can be the predetermined flow value of the gas of the entering sulfur dioxide air blast 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) control the gas flow that gets into the sulfur dioxide air blast according to the result of said comparison and provide to the pressure of the gas of sulphuric acid plant from the sulfur dioxide air blast.This step can realize through the switch 55 and the gas flow control valve 53 of second control element 54, sulfur dioxide air blast.Second control element 54 receives flow measuring element 51 and/or pressure measuring element 52 is measured data on flows and/or pressure data in real time; Measured then real time data and target data compare; If real time data is greater than the target data of correspondence; Then control the switch 55 and gas flow control valve 53 of sulfur dioxide air blast, adjust, until near target data with flow and/or pressure to gas.Here, second control element can repeatedly be adjusted data on flows and/or pressure data, until the flow of gas and/or pressure near or equal corresponding target data.
In sum; The control system and method that is used for renewable flue gas desulphurization system according to the present invention can be controlled at the vapor (steam) temperature that gets into reboiler in the scope of technological requirement; Thereby reduced reboiler incrustation; Improve heat exchange efficiency and steam utilization, and can rationally control the flow and the pressure of the gas that gets into sulfur dioxide air blast and sulphuric acid plant, guaranteed the direct motion of acid-making process.In addition, control system and method for the present invention can also be stablized from the temperature and the flow of reboiler steam that produce and that offer desorber, has guaranteed the desorption technique stable smooth operation of desorber.
Although combined certain exemplary embodiment to describe the present invention above, it will be apparent to those skilled in the art that under the situation of spirit that does not break away from claim and limited and scope, can make amendment and change above-mentioned exemplary embodiment.
Claims (10)
1. a control system that is used for renewable flue gas desulphurization system is characterized in that, said control system comprises reboiler temperature control module and sulfur dioxide air blast control module, wherein,
Said reboiler temperature control module comprises first temperature element, second temperature element, heat sink, steam flow control valve and first control element; Said first temperature element is arranged on to reboiler and provides in the vapour source of thermal source; Said second temperature element is arranged in the Steam area that will heat the desulfuration solution lean solution in the reboiler; Said heat sink is arranged on the steam conveying pipe that connects vapour source and reboiler; Said steam flow control valve is arranged on the said steam conveying pipe; Said first control element is connected with second temperature element to receive the temperature data from first temperature element and second temperature element with first temperature element respectively; And respectively said temperature data and process requirements temperature from first temperature element or second temperature element compared; And said first control element also is connected with the steam flow control valve with the result according to said comparison with heat sink respectively and determines whether starting heat sink and/or the steam flow control valve comes steam is lowered the temperature, so that the temperature of steam is near said process requirements temperature;
Said sulfur dioxide air blast control module comprises flow measuring element, pressure measuring element, gas flow control valve and second control element, and said flow measuring element is arranged on the pipeline that is connected with the air inlet of sulfur dioxide air blast.Said pressure measuring element is arranged on the pipeline that connects sulfur dioxide air blast and sulphuric acid plant; Said gas flow control valve is arranged on the pipeline between the air inlet of flow measuring element and sulfur dioxide air blast, and second control element is connected with flow measuring element, pressure measuring element, gas flow control valve and the switch of sulfur dioxide air blast respectively.
2. the control system that is used for renewable flue gas desulphurization system according to claim 1 is characterized in that,
Said first control element comprises the first data receiving element, first data processing unit and first command unit; Wherein, The first data receiving element is connected with second temperature element with first temperature element respectively, to be used to receive the temperature data from first temperature element and second temperature element; First data processing unit is connected between the first data receiving element and first command unit, be used for respectively with said from first temperature element and second temperature element temperature data and process requirements temperature degree is relatively capable and comparative result is sent to first command unit; First command unit is connected with the steam flow control valve with heat sink respectively;
Said second control element comprises the second data receiving element, second data processing unit and second command unit; Wherein, The second data receiving element is connected with pressure measuring element with flow measuring element respectively, to be used to receive from the data on flows of flow measuring element with from the pressure data of pressure measuring element; Second data processing unit is connected between the second data receiving element and second command unit, to be used for respectively with said data on flows and target flow and with pressure data and goal pressure compares and comparative result is sent to second command unit; Second command unit is connected with the switch of gas flow control valve with the sulfur dioxide air blast respectively.
3. the control system that is used for renewable flue gas desulphurization system according to claim 1 and 2; It is characterized in that; Said first temperature element or second temperature element are thermal resistance or thermocouple; Said flow measuring element is the flowmeter that is applicable to etchant gas, and said pressure measuring element is a gas gauge.
4. root institute claim 1 or 2 described control systems that are used for renewable flue gas desulphurization system; It is characterized in that; Said heat sink comprises condensate liquid storage device and the condensate liquid spray thrower that connects through pipeline, and said condensate liquid spray thrower is arranged in the said steam conveying pipe and has the valve of scalable condensate liquid flow.
5. the control system that is used for renewable flue gas desulphurization system according to claim 2; It is characterized in that; Said first data processing unit comprises first look-up table; Said first look-up table stores has a plurality of first values, said first value representation with from the cooling degree of the corresponding heat sink of the temperature of first temperature element or second temperature element and said process requirements temperature and/or the aperture of steam flow control valve; Said second data processing unit comprises second look-up table; Said second look-up table stores a plurality of second values, said ground two value representations and the comparative result of data on flows and target flow and the aperture of pressing the switch of corresponding gas flow control valve of the data and the comparative result of goal pressure and/or sulfur dioxide air blast.
6. the control method of a control according to claim 1 system is characterized in that, said control method comprises that the reboiler temperature control step of no sequencing controls step with the sulfur dioxide air blast, wherein,
Said reboiler temperature control step comprises: measure the temperature that is about to provide steam to the vapour source of reboiler; The temperature and the process requirements temperature of steam in the said vapour source are compared, when the temperature of steam in the said vapour source is higher than said process requirements temperature, the steam in the said vapour source is lowered the temperature; Measurement gets into the temperature of the steam in the reboiler behind said cooling step; The temperature and the said process requirements temperature that will behind said cooling step, get into the steam in the reboiler compare; The temperature of the steam in behind said cooling step, getting into reboiler is during greater than said process requirements temperature; Reduce to get into the flow of the steam in the reboiler or increase the degree that the steam in the said vapour source is lowered the temperature, so that the temperature of steam approaches said process requirements temperature;
Said sulfur dioxide air blast control step comprises: measurement is about to get into the gas flow of sulfur dioxide air blast and provides to the pressure of the gas of sulphuric acid plant from the sulfur dioxide air blast; Respectively said gas flow and pressure are compared with corresponding flow setting value and pressure set points; Control the gas flow that gets into the sulfur dioxide air blast and provide to the pressure of the gas of sulphuric acid plant according to the result of said comparison from the sulfur dioxide air blast.
7. control method according to claim 6; It is characterized in that; Said reboiler is connected with the desorber of renewable flue gas desulphurization system; Liquid heat will from desorber, flow into reboiler is a steam, and the air inlet of said sulfur dioxide air blast is connected with the sulfur dioxide outlet of drying tower, gas-liquid separator and desorber through pipeline successively.
8. control method according to claim 6 is characterized in that, said process requirements temperature is set at 115 ± 5 ℃.
9. control method according to claim 6 is characterized in that, said cooling step is realized through the steam spray cooling lime set in said vapour source.
10. control method according to claim 6 is characterized in that, the spray flux of said condensate liquid can calculate through the heat exchange efficiency of routine.
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| CN201110416707.7A CN102512917B (en) | 2011-12-14 | 2011-12-14 | Control system for renewable flue gas desulfurization system and control method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103881763A (en) * | 2014-03-26 | 2014-06-25 | 济钢集团有限公司 | Gas desulfurization device |
| CN104208985A (en) * | 2014-09-29 | 2014-12-17 | 长沙华时捷环保科技发展有限公司 | Flue gas desulfurization method and system |
| CN110068489A (en) * | 2019-06-12 | 2019-07-30 | 中冶北方（大连）工程技术有限公司 | Activated coke particle and regeneration gas separating pressure sampler |
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| 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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| JPS59169523A (en) * | 1983-03-15 | 1984-09-25 | Babcock Hitachi Kk | Control of wet waste gas desulfurization apparatus |
| 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 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103881763A (en) * | 2014-03-26 | 2014-06-25 | 济钢集团有限公司 | Gas desulfurization device |
| CN103881763B (en) * | 2014-03-26 | 2015-05-27 | 济钢集团有限公司 | Gas desulfurization device |
| CN104208985A (en) * | 2014-09-29 | 2014-12-17 | 长沙华时捷环保科技发展有限公司 | Flue gas desulfurization method and system |
| CN104208985B (en) * | 2014-09-29 | 2016-08-24 | 长沙华时捷环保科技发展股份有限公司 | Fume desulphurization method and system |
| CN110068489A (en) * | 2019-06-12 | 2019-07-30 | 中冶北方（大连）工程技术有限公司 | Activated coke particle and regeneration gas separating pressure sampler |
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| CN102512917B (en) | 2014-03-26 |
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