CN102872680A - Flue gas desulphurization system and flue gas desulphurization method - Google Patents
Flue gas desulphurization system and flue gas desulphurization method Download PDFInfo
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- CN102872680A CN102872680A CN2012103652173A CN201210365217A CN102872680A CN 102872680 A CN102872680 A CN 102872680A CN 2012103652173 A CN2012103652173 A CN 2012103652173A CN 201210365217 A CN201210365217 A CN 201210365217A CN 102872680 A CN102872680 A CN 102872680A
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Abstract
The invention relates to an energy-saving flue gas desulphurization system and a flue gas desulphurization method. The flue gas desulphurization system comprises: an absorbing tower which comprises a housing, a flue gas inlet for supplying the flue gas into the housing, a barren liquor inlet for supplying the barren liquor containing a desulfurizer into the housing, a clean flue gas outlet for discharging the clean flue gas with sulfur dioxide being removed, and a rich liquor outlet for discharging the rich liquor with sulfur dioxide absorbed at a predetermined temperature; a regeneration tower which comprises a body, a regenerated gas outlet for discharging the regenerated gas, a rich liquor inlet for supplying part of the rich liquor into the body, and a barren liquor outlet located at the body bottom and used for discharging the barren liquor with sulfur dioxide being precipitated, wherein the rich liquor inlet of the regeneration tower is connected with the rich liquor outlet of the absorbing tower, and the barren liquor outlet of the regeneration tower is connected with the barren liquor inlet of the absorbing tower; and a rich liquor circulating pump which is connected with the rich liquor outlet and the barren liquor inlet of the absorbing tower, and is used for returning the other part of the rich liquor discharged from the absorbing tower back to the absorbing tower.
Description
Technical field
The present invention relates to a kind of flue gas desulphurization system and a kind of fume desulphurization method.
Background technology
Sulfur dioxide pollution has become the key factor of restriction China economy, social sustainable development, and it is imperative therefore to control sulfur dioxide pollution.According to environmental protection " 12 " planning, by 2015, SO
2Total emission volumn will reduce to 2086.4 ten thousand tons, and comparing 2010 needs to reduce discharging 8%; Require simultaneously the comprehensive utilization ratio of the industrial solid castoffs such as industrial gypsum will reach 75%, under this background, " limestone-gypsum " desulfur technology that China's desulfuration field is commonly used is subjected to the effects limit such as carbon dioxide discharge-reduction requirement and desulfurated plaster recycling difficulty, will progressively be replaced on a large scale by other desulfur technologies.And, existing take organic amine, ionic liquid, citrate, polymeric absorbent is as absorbent and adopt traditional absorption-thermal regeneration absorbent and prepare high-purity SO
2Flue gas desulfurization technique, exist the problems such as energy consumption is higher, heat is not fully utilized.
Therefore, existing flue gas desulphurization system and fume desulphurization method have much room for improvement.
Summary of the invention
The present invention is intended to one of solve the problems of the technologies described above at least.For this reason, the present invention proposes a kind of energy-conservation flue gas desulphurization system and a kind of energy-conservation fume desulphurization method.
According to an aspect of the present invention, provide a kind of flue gas desulphurization system.Described flue gas desulphurization system comprises: absorption tower, described absorption tower comprise housing, be used for flue gas supply to smoke inlet in the described housing, the lean solution that is used for containing desulfurizing agent supplies to lean solution entrance in the described housing, be used for discharging the clean exhanst gas outlet of the clean flue gas of sloughing sulfur dioxide and being used for discharging the rich solution outlet that has absorbed the rich solution of sulfur dioxide at predetermined temperature; Regenerator, described regenerator comprises body, is used for the regeneration gas outlet of discharge regeneration gas, is used for a part of rich solution is supplied to described intrinsic rich solution entrance, is positioned at described body bottom and is used for the lean solution outlet that discharge parses the lean solution of sulfur dioxide, the rich solution entrance of wherein said regenerator links to each other with the outlet of the rich solution on described absorption tower, and the lean solution outlet of regenerator links to each other with the lean solution entrance on described absorption tower; With the rich solution circulating pump, described rich solution circulating pump links to each other with the lean solution entrance with the rich solution outlet on described absorption tower, is used for making another part rich solution of discharging from described absorption tower to return described absorption tower.
According to the flue gas desulphurization system of the embodiment of the invention, can be according to SO in the flue gas
2Concentration height situation, only send a part of rich solution to regenerate, another part rich solution then continues circulation in the absorption tower, thereby the load that can alleviate like this regenerator with thermal source (for example reduces regeneration, saturated vapor) consumption, can guarantee also that simultaneously the absorption tower satisfies the required absorption liquid sprinkle density of desulfuration efficiency, such as reducing equipment investment and the energy consumptions such as regenerator, poor rich liquid heat exchanger, reduce cost thus.
In one embodiment of the invention, described flue gas desulphurization system further comprises the rich solution reheater, described rich solution reheater exports with regeneration gas with the rich solution entrance of described regenerator and links to each other, be used for making from the rich solution of described absorption tower discharge and from the regeneration gas that described regenerator is discharged and carry out heat exchange, cool off thereby the rich solution of discharging from described absorption tower is heated up and make from the regeneration gas of described regenerator discharge.Thus, reclaim first part heat from the regeneration gas that regenerator is discharged with the rich solution of discharging from the absorption tower, the temperature that had so both improved rich solution is beneficial to regeneration and reduces the consumption that steam is used in regeneration, also reduced simultaneously the consumption that cools off the required cooling water of regeneration gas, reduce thus energy consumption, energy savings.
In one embodiment of the invention, described regenerator further comprises the semi lean solution outlet that is positioned at lean solution outlet top, is used for discharging the semi lean solution that parses sulfur dioxide, and supplies to the semi lean solution entrance in the regenerator after being used for again heating up from the semi lean solution that the semi lean solution outlet is discharged; Described flue gas desulphurization system further comprises for again heating up from export the reboiler of the semi lean solution of discharging at the semi lean solution of regenerator, the entrance that boils again of wherein said reboiler links to each other with the semi lean solution outlet of regenerator, the outlet of boiling again of described reboiler links to each other with the semi lean solution entrance of regenerator, and described reboiler also comprises high-temperature flue gas entry, high-temperature flue gas outlet, saturated vapor entrance and saturated vapor outlet.
In one embodiment of the invention, described flue gas comprises that temperature is the high-temperature flue gas that 90 ~ 110 degrees centigrade low-temperature flue gas and temperature are 120 ~ 300 degrees centigrade.
In one embodiment of the invention, described reboiler also links to each other with the smoke inlet on described absorption tower, is used for described high-temperature flue gas is cooled to 90 ~ 110 degrees centigrade and cooled flue gas supplied in the described absorption tower.Thus, semi lean solution is cooled to 90 ~ 110 degrees centigrade (for example, 105 degrees centigrade) thereby high-temperature flue gas at first enters the reboiler heating, then just can directly send into the absorption tower.With respect to traditional desulphurization system, according to the flue gas desulphurization system of the embodiment of the invention, both can by utilizing the consumption of the heat minimizing regeneration steam in the flue gas, can reduce again the production water consumption that flue gas desulphurization system causes because of evaporation, reduce thus energy consumption, energy savings.
In one embodiment of the invention, described flue gas desulphurization system further comprises poor rich liquid heat exchanger, described poor rich liquid heat exchanger links to each other with the rich solution entrance of described regenerator with the rich solution outlet on described absorption tower respectively, and link to each other with the lean solution entrance on described absorption tower with the outlet of the lean solution of described regenerator respectively, thereby so that the rich solution of discharging from described absorption tower and the lean solution of discharging from described regenerator are carried out heat exchange the rich solution of discharging from described absorption tower is heated up and make from the lean solution of described regenerator discharge and lower the temperature.
In one embodiment of the invention, described flue gas desulphurization system further comprises and is used between the rich solution outlet that is connected to described absorption tower and the described poor rich liquid heat exchanger rich solution in the described absorption tower is delivered to rich solution excavationg pump in the described poor rich liquid heat exchanger, and is connected between the lean solution entrance on described absorption tower and the described poor rich liquid heat exchanger for the lean pump of lean solution being delivered in the absorption tower.
In one embodiment of the invention, described flue gas desulphurization system comprises that further described pretreatment unit links to each other with the smoke inlet on described absorption tower for described flue gas being carried out the pretreatment unit of preliminary treatment with the dustiness that reduces described flue gas.
In one embodiment of the invention, described regenerator further comprises reflux inlet, and described flue gas desulphurization system further comprises: condenser, and described condenser and the regeneration gas that the regeneration gas outlet of regenerator links to each other and discharges from regenerator with condensation obtain sulfur dioxide gas and condensate liquid; With the gas-liquid separator of the sulfur dioxide gas that obtains for separating of condensation and condensate liquid, described gas-liquid separator links to each other that with described condenser isolated condensate liquid is returned described regenerator with the reflux inlet of described regenerator respectively.
In one embodiment of the invention, described flue gas desulphurization system further comprises reflux pump, and described reflux pump is connected between the reflux inlet of the condensate outlet of described gas-liquid separator and described regenerator and is used for described condensate pump is delivered in the described regenerator.
According to a further aspect in the invention, provide a kind of fume desulphurization method.Described fume desulphurization method may further comprise the steps: with flue gas from the underfeed on absorption tower in described absorption tower; The lean solution that will contain desulfurizing agent supplies in the described absorption tower to contact with described flue gas adverse current from the top on described absorption tower, and the temperature in the described absorption tower is controlled at predetermined temperature so that described desulfurizing agent absorbs the sulfur dioxide in the described flue gas; Discharge the clean flue gas of sloughing sulfur dioxide from top, described absorption tower; Discharge the rich solution that has absorbed sulfur dioxide from bottom, described absorption tower; Supply in the described regenerator from described regenerator top after will heating up from a part of rich solution that discharge on described absorption tower, in order to make described rich solution parse the sulfur dioxide of absorption; Make another part rich solution of discharging from described absorption tower return described absorption tower by the rich solution circulating pump; Parse the lean solution of sulfur dioxide and the sulfur dioxide that parses with discharging from described regenerator.
According to the fume desulphurization method of the embodiment of the invention, can be according to SO in the flue gas
2Concentration height situation, only send a part of rich solution to regenerate, another part rich solution then continues circulation in the absorption tower, thereby the load that can alleviate like this regenerator with thermal source (for example reduces regeneration, saturated vapor) consumption, can guarantee also that simultaneously the absorption tower satisfies the required absorption liquid sprinkle density of desulfuration efficiency, reduce thus equipment investment and energy consumption, reduce cost.
In one embodiment of the invention, described fume desulphurization method further comprises: turn back in the described regenerator after will again heating up from the lean solution that described regenerator is discharged, in order to make described lean solution again parse sulfur dioxide.
In one embodiment of the invention, described desulfurizing agent is be selected from organic amine desulfurizer, renewable macromolecule desulfurizing agent, ionic liquid and citrate at least a; Described organic amine desulfurizer is be selected from fatty amine, piperazine and derivative thereof, pyridine and its derivatives, imidazole and its derivants and the sterically hindered amines such as dimethylaniline, monoethanolamine, diethanol amine, N methyldiethanol amine, diethylenetriamine at least a.
In one embodiment of the invention, described fume desulphurization method further comprises: will turn back in the described absorption tower from the lean solution that described regenerator is discharged, thereby and make and carry out heat exchange from described the regenerator lean solution of discharging and the rich solution of discharging the rich solution of discharging from described absorption tower is heated up and make the lean solution cooling of discharging from described regenerator from described absorption tower.
In one embodiment of the invention, described fume desulphurization method further comprises: the regeneration gas that condensation is discharged from described regenerator top obtains sulfur dioxide gas and condensate liquid; With sulfur dioxide and the condensate liquid that obtains carried out gas-liquid separation, and make isolated condensate liquid return described regenerator.
In one embodiment of the invention, described fume desulphurization method further comprises: the flue gas that supplies in the described absorption tower is carried out preliminary treatment to reduce the dustiness of described flue gas.
In one embodiment of the invention, described predetermined temperature is in 90 ~ 110 degrees centigrade scope.
In one embodiment of the invention, described fume desulphurization method further comprises: make the rich solution of discharging from described absorption tower and the regeneration gas of discharging from described regenerator carry out heat exchange, thereby make the rich solution intensification of discharging from described absorption tower and make the regeneration gas cooling of discharging from described regenerator.Thus, reclaim first part heat from the regeneration gas that regenerator is discharged with the rich solution of discharging from the absorption tower, the temperature that had so both improved rich solution is beneficial to regeneration and reduces the consumption that steam is used in regeneration, also reduced simultaneously the consumption that cools off the required cooling water of regeneration gas, reduce thus energy consumption, energy savings.
In one embodiment of the invention, described flue gas comprises that temperature is the high-temperature flue gas that 90 ~ 110 degrees centigrade low-temperature flue gas and temperature are 120 ~ 300 degrees centigrade.
In one embodiment of the invention, described fume desulphurization method further comprises: described high-temperature flue gas is cooled to 90 ~ 110 degrees centigrade and cooled flue gas supplied in the described absorption tower.Thus, high-temperature flue gas at first enters reboiler heating semi lean solution (sometimes can be called " middle lean solution ") thereby is cooled to 90 ~ 110 degrees centigrade (for example, 105 degrees centigrade), then just can directly send into the absorption tower.With respect to traditional technological process, according to the fume desulphurization method of the embodiment of the invention, both can by utilizing the consumption of the heat minimizing regeneration steam in the flue gas, can reduce again the production water consumption that flue gas desulphurization system causes because of evaporation, reduce thus energy consumption, energy savings.
Additional aspect of the present invention and advantage in the following description part provide, and part will become obviously from the following description, or recognize by practice of the present invention.
Description of drawings
Above-mentioned and/or additional aspect of the present invention and advantage are from obviously and easily understanding becoming the description of embodiment in conjunction with following accompanying drawing, wherein:
Fig. 1 is the schematic diagram according to the flue gas desulphurization system of the embodiment of the invention; With
Fig. 2 is the flow chart according to the fume desulphurization method of the embodiment of the invention;
The specific embodiment
The below describes embodiments of the invention in detail, and the example of described embodiment is shown in the drawings, and wherein identical or similar label represents identical or similar element or the element with identical or similar functions from start to finish.Be exemplary below by the embodiment that is described with reference to the drawings, only be used for explaining the present invention, and can not be interpreted as limitation of the present invention.
In description of the invention, it will be appreciated that, term " " center "; " vertically "; " laterally "; " on "; D score; " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end " " interior ", orientation or the position relationship of indications such as " outward " are based on orientation shown in the drawings or position relationship, only be for convenience of description the present invention and simplified characterization, rather than device or the element of indication or hint indication must have specific orientation, with specific orientation structure and operation, therefore can not be interpreted as limitation of the present invention.
In description of the invention, need to prove that unless clear and definite regulation and restriction are arranged in addition, term " installation ", " linking to each other ", " connection " should be done broad understanding, for example, can be to be fixedly connected with, connect integratedly, also can be to removably connect; Can be mechanical connection or electrical connection, also can be the connection of two element internals; Can be directly to link to each other, also can indirectly link to each other by intermediary, for the ordinary skill in the art, can understand as the case may be the concrete meaning of above-mentioned term.
In addition, in order to understand better the present invention, before describing, the part term that uses in need to describing the present invention is simply explained.The desulfurizing agent that " lean solution " refers to there is not the desulfurizing agent of sulfur dioxide absorption or parsed institute's sulfur dioxide absorption." rich solution " referred to absorb the desulfurizing agent of sulfur dioxide, wherein, if rich solution removes wherein sulfur dioxide by twice above parsing, so in the present invention, after the one parsing and the desulfurizing agent of resolving for the last time before the desulfurization also can be called semi lean solution, last desulfurizing agent of resolving after the desulfurization is called lean solution, if rich solution only removes wherein sulfur dioxide by one parsing, the desulfurizing agent after the one parsing desulfurization just is called lean solution so.
Below with reference to the flue gas desulphurization system of accompanying drawing detailed description according to the embodiment of the invention.
As shown in Figure 1, the flue gas desulphurization system according to the embodiment of the invention mainly comprises absorption tower 1 and regenerator 2.
The flue gas that contains sulfur dioxide 1 bottom is sent into absorption tower 1 from the absorption tower, lean solution 1 top is sent into absorption tower 1 from the absorption tower, lean solution flows downward in absorption tower 1 thus, flue gas is 1 interior to flowing on the absorption tower, the two counter current contacting, thus lean solution with process that flue gas contacts in absorb wherein sulfur dioxide.The clean flue gas that removes sulfur dioxide 1 top is discharged from the absorption tower, and the liquid rich solution that has absorbed sulfur dioxide 1 bottom is discharged from the absorption tower.
1 rich solution of discharging is sent into regenerator 2 after heating up from the absorption tower, in regenerator 2, because temperature raises, rich solution parses the sulfur dioxide that absorbs, become lean solution, and that the lean solution of discharging from regenerator 2 that parses sulfur dioxide turns back to absorption tower 1 through cooling is interior recycling.
As shown in Figure 1, absorption tower 1 comprises housing, smoke inlet, lean solution entrance, clean exhanst gas outlet and rich solution outlet.
The housing on absorption tower 1 is the container of cardinal principle oblong shape along the vertical direction, and inside defines a cavity.The smoke inlet on absorption tower 1 is arranged on the sidewall of lower housing portion on absorption tower 1, and the flue gas that contains sulfur dioxide enters in the absorption tower 1 by the smoke inlet on absorption tower 1.The lean solution entrance on absorption tower 1 arranges on the sidewall on housing top on absorption tower 1, and the lean solution that contains desulfurizing agent enters in the housing on absorption tower 1 by the lean solution entrance on absorption tower 1.The clean exhanst gas outlet on absorption tower 1 is arranged on the top of the housing on absorption tower 1, sloughed clean flue gas behind the sulfur dioxide from the absorption tower 1 exhanst gas outlet discharge absorption tower 1.The outlet of the rich solution on absorption tower 1 is arranged on the bottom of the housing on absorption tower 1, the rich solution that in the housing on absorption tower 1, has absorbed the sulfur dioxide in the flue gas from the absorption tower 1 rich solution outlet discharge absorption tower 1.
In some embodiments of the invention, described desulfurizing agent can have for being selected from organic amine desulfurizer, renewable macromolecule desulfurizing agent, ionic liquid, citrate and other sulfur dioxide absorbent at least a of heating regenerating desulfurization ability; Described organic amine desulfurizer can be for being selected from least a of fatty amine, piperazine and derivative thereof, pyridine and its derivatives, imidazole and its derivants and the sterically hindered amines such as dimethylaniline, monoethanolamine, diethanol amine, N methyldiethanol amine, diethylenetriamine.Above-mentioned desulfurizing agent can be at the predetermined temperature sulfur dioxide absorption, and can the temperature more than predetermined temperature parse sulfur dioxide, for example in 40 ~ 50 degrees centigrade scope, the temperature of desulfurizing agent parsing sulfur dioxide for example can be at 90 ~ 110 degrees centigrade for described predetermined temperature.
Certainly, desulfurizing agent is not limited to above-mentioned concrete example, as long as desulfurizing agent can be under relatively low temperature sulfur dioxide absorption, and resolving sulfur dioxide under relatively high temperature gets final product, the name that for example can use commercially available Chengdu Huaxi Industrial Gas Co., Ltd. to produce is called " ionic liquid desulfurizing agent ", and model is the desulfurizing agent of HXDS01.
As shown in Figure 1, regenerator 2 comprises body, regeneration gas outlet, rich solution entrance, semi lean solution outlet, semi lean solution entrance and lean solution outlet.
The body of regenerator 2 is cardinal principle Long Circle pressure vessel along the vertical direction, and limits a cavity.The regeneration gas outlet of regenerator 2 is arranged on the top of the body of regenerator 2, is used for discharging rich solution parses sulfur dioxide in the body of regenerator 2 regeneration gas.The rich solution entrance of regenerator 2 is arranged on the sidewall on body top of regenerator 2, the rich solution entrance of regenerator 2 links to each other with the outlet of the rich solution on absorption tower 1, the rich solution that 1 part of discharging has absorbed sulfur dioxide from the absorption tower is thus sent into after intensification in the body of regenerator 2, in order to parse the sulfur dioxide of absorption in the body of regenerator 2.
The outlet of the semi lean solution of regenerator 2 is arranged on the sidewall of body of regenerator 2 and is positioned at the below of the rich solution entrance of regenerator 2, the intrinsic rich solution that is sent to regenerator 2 from absorption tower 1 becomes lean solution (semi lean solution) after the intensification one parsing goes out sulfur dioxide, discharge from the lean solution outlet of regenerator 2, but export the body of discharging regenerator 2 by the semi lean solution of regenerator 2.Correspondingly, the semi lean solution entrance of regenerator 2 be arranged at the body of regenerator 2 regenerator 2 the semi lean solution outlet below, the one parsing of discharging from the semi lean solution outlet of regenerator 2 semi lean solution of sulfur dioxide through again heating up (for example by reboiler 5, as shown in Figure 1) the semi lean solution entrance from regenerator 2 turns back in the body of regenerator 2, in order to again parse sulfur dioxide in the body of regenerator 2, the body of regenerator 2 is discharged in the lean solution outlet that again parses the regenerator 2 of lean solution bottom the body that is arranged on regenerator 2 of sulfur dioxide.
The lean solution outlet of regenerator 2 links to each other with the lean solution entrance on absorption tower 1, thereby the lean solution that will parse sulfur dioxide is returned absorption tower 1.
Here, be appreciated that, 1 a part of rich solution of discharging from the absorption tower, send in the body of regenerator 2 by the rich solution entrance of regenerator 2, one parsing becomes semi lean solution after going out part sulfur dioxide, semi lean solution after the one parsing can the semi lean solution outlet by regenerator 2 be discharged the body of regenerator 2, and then the body that returns regenerator 2 from the semi lean solution entrance of regenerator 2 after the heating resolves again, becomes the lean solution that again parses sulfur dioxide.
As shown in Figure 1, in one embodiment of the invention, regenerator 2 may further include reflux inlet, and the reflux inlet of regenerator 2 is arranged on the body of regenerator 2 and is positioned at the regeneration gas outlet below of regenerator 2.The regeneration gas of discharging from the regeneration gas outlet of the bodies top of regenerator 2 contains moisture, therefore can be by condenser 9 and gas-liquid separator 10(as shown in Figure 1) regeneration gas from the regeneration gas outlet discharge of regenerator 2 is carried out condensation and separated, to obtain highly purified sulfur dioxide gas and condensate liquid (for example saturated sulfurous acid solution), condensate liquid can turn back to by the reflux inlet of regenerator 2 in the body of regenerator 2, fully reclaims thus desulfurizing agent.
Flue gas desulphurization system according to the embodiment of the invention also comprises rich solution circulating pump 3.The rich solution outlet on rich solution circulating pump 3 and absorption tower 1 links to each other with the lean solution entrance, and another part rich solution that is used for making from the absorption tower 1 rich solution to export discharge returns absorption tower 1.
According to the flue gas desulphurization system of the embodiment of the invention, can be according to SO in the flue gas
2Concentration height situation, only send a part of rich solution to regenerate, another part rich solution then continues circulation in the absorption tower, thereby the load that can alleviate like this regenerator with thermal source (for example reduces regeneration, saturated vapor) consumption, can guarantee also that simultaneously the absorption tower satisfies the required absorption liquid sprinkle density of desulfuration efficiency, reduce thus equipment investment and energy consumption, reduce cost.With treatment S O
2The flue gas that concentration is about 2000ppm is example, adopts the technological process of sending the part rich solution to regenerate, compares traditional absorption-regeneration technology flow process, and the operating load of regenerative system will reduce by 30% ~ 50%, and corresponding equipment investment and regeneration also reduce with steam consumption.
Flue gas desulphurization system according to the embodiment of the invention further comprises rich solution reheater 4.Rich solution reheater 4 exports with regeneration gas with the rich solution entrance of regenerator 2 and links to each other, be used for making the rich solution of 1 discharge from the absorption tower and the regeneration gas of discharging from regenerator 2 to carry out heat exchange, 1 rich solution of discharging heats up and makes from the regeneration gas cooling of regenerator 2 discharges thereby make from the absorption tower.Thus, reclaim first part heat from the regeneration gas that regenerator is discharged with the rich solution of discharging from the absorption tower, the temperature that had so both improved rich solution is beneficial to regeneration and reduces the consumption that steam is used in regeneration, also reduced simultaneously the consumption that cools off the required cooling water of regeneration gas, reduce thus energy consumption, energy savings.
As mentioned above, the outlet of the rich solution on the absorption tower 1 of flue gas desulphurization system links to each other with the rich solution entrance of regenerator 2, and the lean solution entrance on absorption tower 1 links to each other with the outlet of the lean solution of regenerator 2.In one embodiment of the invention, between absorption tower 1 and regenerator 2, be provided with poor rich liquid heat exchanger 6.Poor rich liquid heat exchanger 6 links to each other with the rich solution entrance of regenerator 2 with the rich solution outlet on absorption tower 1 respectively, and link to each other with the lean solution entrance on absorption tower 1 with the outlet of the lean solution of regenerator 2 respectively, thereby so that from the absorption tower 1 rich solution of discharging and the lean solution of discharging from regenerator 2 carry out heat exchange and make from the absorption tower 1 rich solution of discharging heat up and make from the lean solution of regenerator 2 discharges to lower the temperature.More specifically, the entrance and exit of a path of poor rich liquid heat exchanger 6 links to each other with the rich solution entrance of regenerator 2 with the rich solution outlet on absorption tower 1 respectively, the entrance and exit on poor rich liquid heat exchanger 6 another roads links to each other with the lean solution entrance on absorption tower 1 with the lean solution outlet of regenerator 2 respectively, thereby 1 rich solution of discharging carries out the rich solution intensification that heat exchange makes 1 discharge from the absorption tower thus with the lean solution of discharging from regenerator 2 from the absorption tower, in order to parse sulfur dioxide in regenerator 2, and that the lean solution of discharging from regenerator 2 is sent into absorption tower 1 after by the heat exchange cooling is recycling.
As shown in Figure 1, flue gas desulphurization system further comprises the pretreatment unit 8 that links to each other with the smoke inlet on absorption tower 1, be used for thereby the flue gas that enters absorption tower 1 is carried out the dustiness that preliminary treatment reduces flue gas, for example the fume amount in the flue gas be reduced to 300mg/Nm
3Below.Flue gas on absorption tower 1 upwards with top lower lean solution counter current contacting, thereby the sulfur dioxide in the lean solution absorption flue gas becomes rich solution.The clean flue gas that has removed sulfur dioxide from the absorption tower 1 clean exhanst gas outlet discharge.
Flue gas desulphurization system further comprises and is used between the rich solution outlet that is connected to absorption tower 1 and the poor rich liquid heat exchanger 6 rich solution in the absorption tower 1 is delivered to rich solution excavationg pump 7 in the poor rich liquid heat exchanger 3, and is connected between the lean solution entrance on absorption tower 1 and the poor rich liquid heat exchanger 3 for the lean pump 12 of lean solution being delivered in the absorption tower.
In one embodiment of the invention, described flue gas desulphurization system further comprises for again heating up from the reboiler 5 of the semi lean solution of discharging in the outlet of the semi lean solution of regenerator 2, and wherein the entrance that boils again of reboiler 5 links to each other with the semi lean solution outlet of regenerator 2 and the boiling to export again and link to each other with the semi lean solution entrance of regenerator 2 of reboiler 5.
Rich solution utilizes rich solution excavationg pump 7 to deliver in the poor rich liquid heat exchanger 6 from the rich solution outlet on absorption tower 1, enters regenerator 2 after heating up through heat exchange.
Rich solution after the intensification parses part sulfur dioxide in regenerator 2, become semi lean solution.This semi lean solution is discharged regenerator 2 by semi lean solution outlet, enters reboiler 5 and again heats up by steam, then enters regenerator 2 by the semi lean solution entrance and again resolves desulfurization, thereby can parse more up hill and dale the sulfur dioxide of absorption.The pressure that the thermal source of reboiler 5 can provide for the outside is the steam of 0.3MPa.
In one embodiment of the invention, described flue gas can comprise that temperature is the high-temperature flue gas that 90 ~ 110 degrees centigrade low-temperature flue gas and temperature are 120 ~ 300 degrees centigrade.Reboiler 5 can also link to each other with the smoke inlet on absorption tower 1, is used for described high-temperature flue gas is cooled to 90 ~ 110 degrees centigrade and the smoke inlet of cooled flue gas by absorption tower 1 supplied in the absorption tower 1.Thus, semi lean solution is cooled to 90 ~ 110 degrees centigrade (for example, 105 degrees centigrade) thereby high-temperature flue gas at first enters the reboiler heating, then just can directly send into the absorption tower.With respect to traditional desulphurization system, according to the flue gas desulphurization system of the embodiment of the invention, both can by utilizing the consumption of the heat minimizing regeneration steam in the flue gas, can reduce again the production water consumption that flue gas desulphurization system causes because of evaporation, reduce thus energy consumption, energy savings.Because therefore the heat in the flue gas may adopt this conservation measures also to need special reboiler for desulfurizer regeneration not, this reboiler can be accepted flue gas and two kinds of thermals source of saturated vapor simultaneously.
The sulfur dioxide gas that parses is upwards discharged by the regeneration gas outlet of regenerator 2 together with fractional saturation steam.In one embodiment of the invention, can be connected with condenser 9 and gas-liquid separator 10 in the regeneration gas exit of regenerator 2.Condenser 9 and the regeneration gas that the regeneration gas outlet of regenerator 2 links to each other and discharges from regenerator with condensation obtain sulfur dioxide gas and condensate liquid.Sulfur dioxide gas and condensate liquid that gas-liquid separator 10 obtains for separating of condensation, gas-liquid separator 10 link to each other that with condenser 9 isolated condensate liquid is returned regenerator 2 with the reflux inlet of regenerator 2 respectively.The regeneration gas of discharging from regenerator 2 by condensation in condenser 9 and gas-liquid separator 10 regeneration gas behind the separating and condensing, (for example obtain sulfur dioxide gas and condensate liquid, saturated sulfurous acid solution), condensate liquid from the reflux inlet of regenerator 2 by being connected to gas-liquid separator 10 condensate outlet and the reflux pump 11 between the reflux inlet of regenerator 2 return regenerator 2.In resolving, highly acid salt (for example, sulfate radical and salt acid group) is heat stable salt, can not parse, thereby the sulfur dioxide product has extreme high purity (for example, butt is more than 99%).Highly purified sulfur dioxide gas can be for the production of the good raw material of sulfur dioxide liquid, sulfuric acid, sulphur and other chemical products.
The lean solution of falling regenerator 2 bottoms enters poor rich liquid heat exchanger 6 and carries out heat exchange, and it is recycling to return absorption tower 1 by lean pump 12 from the lean solution entrance after the cooling.
In one embodiment of the invention, flue gas desulphurization system can also comprise lean solution cooler 13.Lean solution cooler 13 is connected between the lean solution entrance on lean pump 12 and absorption tower 1, is used for the lean solution that further cooling is discharged from the lean solution outlet of regenerator 2.
In one embodiment of the invention, 1 lean solution porch can also arrange cleaning equipment 14 on the absorption tower, and for example demineralization plant is used for the lean solution that supplies in the absorption tower 1 is purified.Cleaning equipment 14 is mainly used in removing flue gas and is brought into solid matter in the desulfurizing agent, organic substance, anion, cation etc.In one embodiment of the invention, the capital equipment of cleaning equipment 14 is comprised of front filter, adsorption tank, after-filter, salting out tank, clarifier etc.Front filter, after-filter are mainly used in removing the solid impurity in the solution; Adsorption tank is mainly used in removing the organic impurities in the solution; Salting out tank, clarifier etc. mainly remove anionic impurity and the cation impurity in the solution, and the desulfurizing agent after purifying can enter in the system of the present invention and continue to recycle.
Below with reference to the fume desulphurization method of Fig. 2 description according to the embodiment of the invention.
At first, with flue gas from the underfeed on absorption tower in described absorption tower.Temperature is lower (for example, 40 ~ 50 degrees centigrade) the lean solution that contains desulfurizing agent supply in the described absorption tower to contact with described flue gas adverse current from the top on described absorption tower, and the temperature in the described absorption tower is controlled at predetermined temperature, for example, in 90 ~ 110 degrees centigrade scope, so that described desulfurizing agent absorbs the sulfur dioxide in the described flue gas.In described absorption tower, lean solution contacts with flue gas adverse current carries out desulfurization, and lean solution becomes rich solution after having absorbed the sulfur dioxide in the flue gas.Reach thus the purpose that removes sulfur dioxide in flue gas, and the clean flue gas water content after purifying is higher, the flue gas that substantially reaches capacity can enter atmosphere through the tail gas funnel at top, described absorption tower.
In some embodiments of the invention, described desulfurizing agent can have for being selected from organic amine desulfurizer, renewable macromolecule desulfurizing agent, ionic liquid, citrate and other sulfur dioxide absorbent at least a of heating regenerating desulfurization ability; Described organic amine desulfurizer can be for being selected from least a of fatty amine, piperazine and derivative thereof, pyridine and its derivatives, imidazole and its derivants and the sterically hindered amines such as dimethylaniline, monoethanolamine, diethanol amine, N methyldiethanol amine, diethylenetriamine.Certainly, desulfurizing agent is not limited to above-mentioned concrete example, if desulfurizing agent can be under relatively low temperature sulfur dioxide absorption, and under relatively high temperature, resolve sulfur dioxide and get final product.
In one embodiment of the invention, before flue gas enters the absorption tower, can also carry out preliminary treatment to reduce the dustiness of described flue gas to the flue gas that supplies in the described absorption tower.
Then, discharge the rich solution that has absorbed sulfur dioxide from bottom, described absorption tower.Supply in the described regenerator from described regenerator top after will heating up from a part of rich solution that discharge on described absorption tower, in order to make described rich solution parse the sulfur dioxide of absorption.Make another part rich solution of discharging from described absorption tower return described absorption tower by the rich solution circulating pump, in other words, another part rich solution is discharged at the bottom of the absorption tower and is returned the absorption cat head by the rich solution circulating pump, to guarantee liquid spraying density required in the absorption tower.
Particularly, to be transported to the poor rich liquid heat exchanger from a part of rich solution that discharge on described absorption tower by the rich solution excavationg pump, heat up, be warming up to the top that enters regenerator after about 100 degrees centigrade, carry out one parsing to parse the sulfur dioxide of absorption, the rich solution that one parsing goes out sulfur dioxide becomes semi lean solution.Described semi lean solution enters reboiler, turn back in the described regenerator after again heating up and again resolve, described semi lean solution becomes lean solution, become gas phase and obtain lean solution thereby more up hill and dale sulfur dioxide is parsed, the regeneration gas that will contain the sulfur dioxide that parses is discharged described regenerator from the regeneration gas outlet of described regenerator, and described lean solution is discharged described regenerator from the lean solution outlet of described regenerator.
According to the fume desulphurization method of the embodiment of the invention, can be according to SO in the flue gas
2Concentration height situation, only send a part of rich solution to regenerate, another part rich solution then continues circulation in the absorption tower, thereby the load that can alleviate like this regenerator with thermal source (for example reduces regeneration, saturated vapor) consumption, can guarantee also that simultaneously the absorption tower satisfies the required absorption liquid sprinkle density of desulfuration efficiency, reduce thus equipment investment and energy consumption, reduce cost.
In one embodiment of the invention, the lean solution of discharging from described regenerator can also be turned back in the described absorption tower, thereby and make and carry out heat exchange from described the regenerator lean solution of discharging and the rich solution of from described absorption tower, discharging and the rich solution of discharging from described absorption tower is heated up and make the lean solution cooling of discharging from described regenerator.In one embodiment of the invention, can also further cool off the lean solution after the heat exchange of discharging from the lean solution outlet of regenerator.
In one embodiment of the invention, can also make the rich solution of discharging from described absorption tower and the regeneration gas of discharging from described regenerator carry out heat exchange, thereby make the rich solution intensification of discharging from described absorption tower and make the regeneration gas cooling of discharging from described regenerator.Thus, reclaim first part heat from the regeneration gas that regenerator is discharged with the rich solution of discharging from the absorption tower, the temperature that had so both improved rich solution is beneficial to regeneration and reduces the consumption that steam is used in regeneration, also reduced simultaneously the consumption that cools off the required cooling water of regeneration gas, reduce thus energy consumption, energy savings.
In one embodiment of the invention, described flue gas can comprise that temperature is the high-temperature flue gas that 90 ~ 110 degrees centigrade low-temperature flue gas and temperature are 120 ~ 300 degrees centigrade.Described high-temperature flue gas is cooled to 90 ~ 110 degrees centigrade and cooled flue gas supplied in the described absorption tower.Thus, semi lean solution is cooled to 90 ~ 110 degrees centigrade (for example, 105 degrees centigrade) thereby high-temperature flue gas at first enters the reboiler heating, then just can directly send into the absorption tower.With respect to traditional technological process, according to the fume desulphurization method of the embodiment of the invention, both can by utilizing the consumption of the heat minimizing regeneration steam in the flue gas, can reduce again the production water consumption that flue gas desulphurization system causes because of evaporation, reduce thus energy consumption, energy savings.
In one embodiment of the invention, the regeneration gas that all right condensation is discharged from described regenerator top obtains sulfur dioxide gas and condensate liquid; With sulfur dioxide and the condensate liquid that obtains carried out gas-liquid separation, and make isolated condensate liquid return described regenerator.Thus, obtain highly purified sulfur dioxide gas and can be used as the good raw material of producing sulfur dioxide liquid, sulfuric acid, sulphur and other chemical products.
In one embodiment of the invention, can also purify lean solution, be brought into solid matter in the desulfurizing agent, organic substance, anion, cation etc. to remove flue gas, make desulfurizing agent after the purification can enter system and continue to recycle.
In the description of this specification, the description of reference term " embodiment ", " some embodiment ", " example ", " concrete example " or " some examples " etc. means to be contained at least one embodiment of the present invention or the example in conjunction with specific features, structure, material or the characteristics of this embodiment or example description.In this manual, the schematic statement of above-mentioned term not necessarily referred to identical embodiment or example.And the specific features of description, structure, material or characteristics can be with suitable mode combinations in any one or more embodiment or example.
Although illustrated and described embodiments of the invention, those having ordinary skill in the art will appreciate that: can carry out multiple variation, modification, replacement and modification to these embodiment in the situation that does not break away from principle of the present invention and aim, scope of the present invention is limited by claim and equivalent thereof.
Claims (20)
1. a flue gas desulphurization system is characterized in that, comprising:
Absorption tower, described absorption tower comprise housing, be used for flue gas supply to smoke inlet in the described housing, the lean solution that is used for containing desulfurizing agent supplies to lean solution entrance in the described housing, be used for discharging the clean exhanst gas outlet of the clean flue gas of sloughing sulfur dioxide and being used for discharging the rich solution outlet that has absorbed the rich solution of sulfur dioxide at predetermined temperature;
Regenerator, described regenerator comprises body, is used for the regeneration gas outlet of discharge regeneration gas, is used for a part of rich solution is supplied to described intrinsic rich solution entrance, is positioned at described body bottom and is used for the lean solution outlet that discharge parses the lean solution of sulfur dioxide, the rich solution entrance of wherein said regenerator links to each other with the outlet of the rich solution on described absorption tower, and the lean solution outlet of regenerator links to each other with the lean solution entrance on described absorption tower; With
The rich solution circulating pump, described rich solution circulating pump links to each other with the lean solution entrance with the rich solution outlet on described absorption tower, is used for making another part rich solution of discharging from described absorption tower to return described absorption tower.
2. flue gas desulphurization system according to claim 1, it is characterized in that, further comprise the rich solution reheater, described rich solution reheater exports with regeneration gas with the rich solution entrance of described regenerator and links to each other, be used for making from the rich solution of described absorption tower discharge and from the regeneration gas that described regenerator is discharged and carry out heat exchange, cool off thereby the rich solution of discharging from described absorption tower is heated up and make from the regeneration gas of described regenerator discharge.
3. flue gas desulphurization system according to claim 1, it is characterized in that, described regenerator further comprises the semi lean solution outlet that is positioned at lean solution outlet top, is used for discharging the semi lean solution that parses sulfur dioxide, to export the semi lean solution entrance that will supply to after the semi lean solution of discharging heat up again in the regenerator from semi lean solution with being used for
Described flue gas desulphurization system further comprises for again heating up from export the reboiler of the semi lean solution of discharging at the semi lean solution of regenerator, the entrance that boils again of wherein said reboiler links to each other with the semi lean solution outlet of regenerator, the outlet of boiling again of described reboiler links to each other with the semi lean solution entrance of regenerator, and described reboiler also comprises high-temperature flue gas entry, high-temperature flue gas outlet, saturated vapor entrance and saturated vapor outlet.
4. flue gas desulphurization system according to claim 3 is characterized in that, described flue gas comprises that temperature is the high-temperature flue gas that 90 ~ 110 degrees centigrade low-temperature flue gas and temperature are 120 ~ 300 degrees centigrade.
5. flue gas desulphurization system according to claim 4 is characterized in that, described reboiler also links to each other with the smoke inlet on described absorption tower, is used for described high-temperature flue gas is cooled to 90 ~ 110 degrees centigrade and cooled flue gas supplied in the described absorption tower.
6. flue gas desulphurization system according to claim 1, it is characterized in that, further comprise poor rich liquid heat exchanger, described poor rich liquid heat exchanger links to each other with the rich solution entrance of described regenerator with the rich solution outlet on described absorption tower respectively, and link to each other with the lean solution entrance on described absorption tower with the outlet of the lean solution of described regenerator respectively, thereby so that the rich solution of discharging from described absorption tower and the lean solution of discharging from described regenerator are carried out heat exchange the rich solution of discharging from described absorption tower is heated up and make from the lean solution of described regenerator discharge and lower the temperature.
7. flue gas desulphurization system according to claim 6, it is characterized in that, further comprise being used between the rich solution outlet that is connected to described absorption tower and the described poor rich liquid heat exchanger rich solution in the described absorption tower is delivered to rich solution excavationg pump in the described poor rich liquid heat exchanger, and be connected between the lean solution entrance on described absorption tower and the described poor rich liquid heat exchanger for the lean pump of lean solution being delivered in the absorption tower.
8. flue gas desulphurization system according to claim 1 is characterized in that, comprises that further described pretreatment unit links to each other with the smoke inlet on described absorption tower for described flue gas being carried out the pretreatment unit of preliminary treatment with the dustiness that reduces described flue gas.
9. flue gas desulphurization system according to claim 1 is characterized in that, described regenerator further comprises reflux inlet, and described flue gas desulphurization system further comprises:
Condenser, described condenser and the regeneration gas that the regeneration gas outlet of regenerator links to each other and discharges from regenerator with condensation obtain sulfur dioxide gas and condensate liquid; With
The sulfur dioxide gas that obtains for separating of condensation and the gas-liquid separator of condensate liquid, described gas-liquid separator links to each other that with described condenser isolated condensate liquid is returned described regenerator with the reflux inlet of described regenerator respectively.
10. flue gas desulphurization system according to claim 9, it is characterized in that, further comprise reflux pump, described reflux pump is connected between the reflux inlet of the condensate outlet of described gas-liquid separator and described regenerator and is used for described condensate pump is delivered in the described regenerator.
11. a fume desulphurization method is characterized in that, may further comprise the steps:
With flue gas from the underfeed on absorption tower in described absorption tower;
The lean solution that will contain desulfurizing agent supplies in the described absorption tower to contact with described flue gas adverse current from the top on described absorption tower, and the temperature in the described absorption tower is controlled at predetermined temperature so that described desulfurizing agent absorbs the sulfur dioxide in the described flue gas;
Discharge the clean flue gas of sloughing sulfur dioxide from top, described absorption tower;
Discharge the rich solution that has absorbed sulfur dioxide from bottom, described absorption tower;
Supply in the described regenerator from described regenerator top after will heating up from a part of rich solution that discharge on described absorption tower, in order to make described rich solution parse the sulfur dioxide of absorption;
Make another part rich solution of discharging from described absorption tower return described absorption tower by the rich solution circulating pump; With
Parse the lean solution of sulfur dioxide and the sulfur dioxide that parses from described regenerator discharge.
12. fume desulphurization method according to claim 11 is characterized in that, further comprises:
Turn back in the described regenerator after will again heating up from the lean solution that described regenerator is discharged, in order to make described lean solution again parse sulfur dioxide.
13. fume desulphurization method according to claim 11 is characterized in that, described desulfurizing agent is be selected from organic amine desulfurizer, renewable macromolecule desulfurizing agent, ionic liquid and citrate at least a; Described organic amine desulfurizer is be selected from dimethylaniline, monoethanolamine, diethanol amine, N methyldiethanol amine, diethylenetriamine, piperazine and derivative thereof, pyridine and its derivatives, imidazole and its derivants and sterically hindered amines at least a.
14. fume desulphurization method according to claim 11 is characterized in that, further comprises:
To turn back in the described absorption tower from the lean solution that described regenerator is discharged, thereby and make and carry out heat exchange from described the regenerator lean solution of discharging and the rich solution of from described absorption tower, discharging and the rich solution of discharging from described absorption tower is heated up and make the lean solution cooling of discharging from described regenerator.
15. fume desulphurization method according to claim 10 is characterized in that, further comprises:
The regeneration gas that condensation is discharged from described regenerator top obtains sulfur dioxide gas and condensate liquid; With
Sulfur dioxide and the condensate liquid that obtains carried out gas-liquid separation, and make isolated condensate liquid return described regenerator.
16. fume desulphurization method according to claim 11 is characterized in that, further comprises: the flue gas that supplies in the described absorption tower is carried out preliminary treatment to reduce the dustiness of described flue gas.
17. fume desulphurization method according to claim 11 is characterized in that, described predetermined temperature is in 90 ~ 110 degrees centigrade scope.
18. fume desulphurization method according to claim 11 is characterized in that, further comprises:
Make the rich solution of discharging from described absorption tower and the regeneration gas of discharging from described regenerator carry out heat exchange, thereby make the rich solution intensification of discharging from described absorption tower and make the regeneration gas cooling of discharging from described regenerator.
19. fume desulphurization method according to claim 11 is characterized in that, described flue gas comprises that temperature is the high-temperature flue gas that 90 ~ 110 degrees centigrade low-temperature flue gas and temperature are 150 ~ 300 degrees centigrade.
20. fume desulphurization method according to claim 19 is characterized in that, further comprises:
Described high-temperature flue gas is cooled to 90 ~ 110 degrees centigrade and cooled flue gas supplied in the described absorption tower.
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| CN105056711A (en) * | 2015-08-21 | 2015-11-18 | 马鞍山艺诚机电有限公司 | Multi-stage nested absorption-analysis citrate process for purifying SO2 in smoke |
| CN105148683A (en) * | 2015-08-21 | 2015-12-16 | 马鞍山艺诚机电有限公司 | Citrate process for purifying SO2 in smoke through negative-pressure multi-stage nested absorption and desorption |
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| CN107930346A (en) * | 2017-10-17 | 2018-04-20 | 广西金川有色金属有限公司 | A kind of ionic liquid thermal regeneration device |
| CN109126386A (en) * | 2018-09-21 | 2019-01-04 | 太原师范学院 | A kind of method of the absorbent and application and absorbent regeneration of sulfur dioxide absorption |
| CN110523222A (en) * | 2019-08-16 | 2019-12-03 | 中国能源建设集团广东省电力设计研究院有限公司 | A kind of amine absorbent purification system and smoke carbon dioxide capture system |
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