CN102302894B - Renewable flue gas desulphurization process - Google Patents

Renewable flue gas desulphurization process Download PDF

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CN102302894B
CN102302894B CN 201110210049 CN201110210049A CN102302894B CN 102302894 B CN102302894 B CN 102302894B CN 201110210049 CN201110210049 CN 201110210049 CN 201110210049 A CN201110210049 A CN 201110210049A CN 102302894 B CN102302894 B CN 102302894B
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China
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solution
flue gas
desorption
renewable
rich
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CN 201110210049
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Chinese (zh)
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CN102302894A (en
Inventor
段向东
张开坚
张初永
黎建明
杨秀亮
邱正秋
朱玉萍
王建山
任毅
陈翀
罗义文
罗强
姚钦国
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攀钢集团攀枝花钢钒有限公司
攀钢集团有限公司
攀钢集团研究院有限公司
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Abstract

The invention provides a renewable flue gas desulphurization process. The renewable flue gas desulphurization process comprises an absorption process and a desorption process. In the absorption process, the following steps are sequentially carried out according to the flowing direction of flue gas: absorbing oxysulfide in the flue gas by using a half-lean solution to form a first pregnant solution; further absorbing the oxysulfide in the flue gas by using a lean solution to form a second pregnant solution; catching a desulfuration solution carried in the flue gas by using a detergent; and discharging clean flue gas. The desorption process comprises the following steps of: carrying out first desorption on part of the first pregnant solution to form a half-lean solution and desorption gases; simultaneously carrying out second desorption on part of the first pregnant solution and part of the half-lean solution to form a lean solution and desorption gases; condensing and recycling oxysulfide in the desorption gases; and respectively supplying the other part of the half-lean solution and the lean solution for the absorption process so as to realize the circulation of the desulfuration solution between the absorption process and the desorption process. The renewable flue gas desulphurization process is suitable for processing various oxysulfide-contained flue gases or industrial waste gases.

Description

A kind of renewable flue gas desulphurization process

Technical field

The present invention relates to chemical industry, thermoelectricity and metallurgical technology field, more particularly, relate to a kind of renewable flue gas desulphurization process.

Background technology

At present, the business website of Kang Shifu (cansolv) Co., Ltd ( Http:// www.cansolv.com/cn / so2scrubbingschema.ch2) on but a kind of flue gas desulfurization technique of desorb is disclosed.At first this technique utilize the sulfur dioxide in the amine absorption flue gas, then the sulfur dioxide in desorb amine liquid at high temperature, with the sulfur dioxide gas of acquisition higher degree, and the amine liquid of the sulfur dioxide absorption ability that is restored simultaneously, described amine liquid can recycle.At present, but also have a kind of process of ionic liquid Desorption desulphurization, this technical process is substantially similar to the process of above-mentioned amine method desulphurization technological process.Difference both is that desulfurization absorption liquid component is different, and the ability of its sulfur dioxide absorption is basically identical.The one-level absorption that above-mentioned two kinds of sulfur removal technologies all adopt and the desorption technique of one-level desorb, in addition, they have optionally adopted flue gas prewashing technique according to the dustiness situation in flue gas to be desulfurization, and they all adopt traditional resin desalinating process to the recovery processing of desulfuration solution.

At present, the sulfur removal technology of prior art has many deficiencies, and main manifestations is: in desulfuration solution, suspended impurity content is high, system jams is serious, desulfurization degree is low, the desorb energy consumption is large, desulfuration solution Difficulty of CR, strong acid root removal efficiency are low etc.In addition, have the highly acid gas contents such as dust content is large, sulfur trioxide, chlorine, nitrate anion due to the sinter fume in metallurgical industry than high, so when the sulfur dioxide gas in the sinter fume that the sulfur removal technology with prior art removes, above-mentioned deficiency will be more serious, and the former thereby defective such as resin desalting effect that cause is poor and the desulfuration solution loss is large such as can further to occur when using resin to remove chlorine root, nitrate anion under high-load sulfate radical condition that Choice of Resin is poor, resin is loaded large.Simultaneously, flue gas desulphurization system carries moisture content secretly because of flue gas and resin desalination washings fill into desulphurization system, causes the increase of the desulphurization system water yield, and how effectively reducing system's water yield is that desulfuration solution concentration keeps certain key.

Summary of the invention

Above-mentioned deficiency for prior art the invention provides a kind of renewable flue gas desulphurization process, to solve one or more deficiency of the prior art.

The invention provides a kind of renewable flue gas desulphurization process, described renewable flue gas desulphurization process comprises by the absorption technique that absorbs the oxysulfide that contains in flue gas with desulfuration solution with by heating and comes desorb to be absorbed with the desulfuration solution of oxysulfide with the desorption technique of recovery oxysulfide, wherein, described absorption technique comprises the following steps of carrying out successively by the flow of flue gas direction: (i) use the oxysulfide in the first desulfuration solution absorption flue gas, form the first rich solution; (ii) use the second desulfuration solution further to absorb oxysulfide in flue gas, form the second rich solution, with the second rich solution as the second desulfuration solution or as the first desulfuration solution; (iii) use washing agent to capture the desulfuration solution of carrying secretly in flue gas; (iv) discharge clean flue gas; Described desorption technique comprises the following steps: (a) part of the first rich solution is carried out a desorb, form semi lean solution and desorption gas; (b) simultaneously another part of the first rich solution and the part of semi lean solution are carried out the secondary desorb, form lean solution and desorption gas; (c) condensation and reclaim oxysulfide in desorption gas; Another part of semi lean solution as the first desulfuration solution, and is provided lean solution respectively to absorption technique as the second desulfuration solution, to realize the circulation of desulfuration solution between absorption technique and desorption technique; The oxysulfide content of described the first rich solution or the second rich solution is higher than the oxysulfide content of semi lean solution, and the oxysulfide content of described semi lean solution is higher than the oxysulfide content of lean solution.

Compared with prior art, renewable flue gas desulphurization process of the present invention comprises that flue gas washing step, absorption technique, desorption technique, desulfuration solution purify recovery technique, thereby can improve desulfurized effect, (for example reduce the desorb energy consumption, system of the present invention can reduce reboiler energy consumption about 35%), prevent system jams, reduce the desulfuration solution loss, and can adapt to the absorbent absorption characteristic, and technique of the present invention can be applicable to various flue gas or the industrial waste gases that contain oxysulfide (for example, sulfur dioxide and sulfur trioxide).For example, renewable flue gas desulphurization process of the present invention can be applied to the field that sintered discharge gas, blast furnace gas, coke-stove gas, coal-fired plant boiler waste gas, heating furnace waste gas etc. need to carry out the exhuast gas desulfurization processing and reclaim.

Description of drawings

By the description of carrying out with reference to the accompanying drawings, above and other purpose of the present invention and characteristics will become apparent, in accompanying drawing:

Figure 1A shows a kind of schematic diagram for realizing the device of the renewable flue gas desulphurization process of the first exemplary embodiment according to the present invention;

Figure 1B illustrates the renewable flue gas desulphurization process schematic diagram of the first exemplary embodiment according to the present invention;

Fig. 2 A shows a kind of schematic diagram for realizing according to the device of the renewable flue gas desulphurization process of inventing the second exemplary embodiment;

Fig. 2 B shows the renewable flue gas desulphurization process schematic diagram according to invention the second exemplary embodiment.

Main Reference numeral:

100: absorption system 110: semi lean solution absorber portion 111: the semi lean solution entrance

113: the first flue gases of rich solution outlet in 112: the first rise 114: the first packing layers of gas hood

115: 116: the first rich solution grooves 120 of first liquid distributor: lean solution absorber portion

121: 123: the second flue gases of lean solution entrance rich solution outlet in 122: the second rise gas hood

Packing layer 125 in 124: the second: 126: the second rich solution grooves of second liquid distributor

130: desulfuration solution captures section 131: cleaning solution entrance 132: the trapping solution outlet

Three flue gases rose 135: the three liquid distribution troughs of 134: the three packing layers of gas hood in 133: the

136: capture liquid bath 137: circulating pump

200: 211: the first rich solution entrances of 210: the first stripping stages of desorption system

212: 213: the first desorption gas of semi lean solution outlet rise 214: the four packing layers of gas hood

215: the four liquid distribution troughs 216: 220: the second stripping stages of semi lean solution storage tank

221: the second rich solution entrances 222: 223: the second desorption gas of lean solution outlet rise gas hood

225: the five liquid distribution troughs 226 of 224: the five packing layers: lean solution storage tank

230: reboiler 230 ': the second reboiler 240: desorber demist layer 250: dividing plate

300: desulfuration solution purifies resuscitation system 310: sedimentation filtration system 320: the freezing and crystallizing system

330: the resin desalination system

430: the three pipelines of 420: the second pipelines of 410: the first pipelines

413: the second poor rich liquid heat exchangers of 412: the first poor rich liquid heat exchangers

500: the flue gas washing system

600: the desorption gas treatment system

The specific embodiment

In order to understand better the present invention, before embodiment was described in detail, the part term that uses in need to describing the present invention was simply explained.In this manual, sulfur-containing smoke gas to be desulfurization (hereafter is flue gas) comprises at least a in sinter fume, metallurgical gas, flue gas in power station boiler etc., and oxysulfide wherein is mainly sulfur dioxide.in this specification, " desulfuration solution " refers to (comprise sulfur dioxide and sulfur trioxide for the oxysulfide that removes flue gas, hereinafter, take sulfur dioxide as example) solution, " desulfuration solution rich solution " (following referred to as " rich solution ") referred to absorb the desulfuration solution of sulfur dioxide, " desulfuration solution lean solution " (following referred to as " lean solution ") refers to there is no the desulfuration solution of sulfur dioxide absorption or separated the desulfuration solution of the sulfur dioxide that sucking-off absorbs, wherein, if desulfuration solution is deviate from the sulfur dioxide of absorption by twice above desorb, after Desorption desulphurization first and the last time the desulfuration solution before Desorption desulphurization can be called " desulfuration solution semi lean solution " (below referred to as " semi lean solution "), desulfuration solution after last Desorption desulphurization is " lean solution ", if the sulfur dioxide that the desulfuration solution rich solution is only deviate to absorb by a desorb, the desulfuration solution after Desorption desulphurization just can become " lean solution " so.Therefore, the oxysulfide content of semi lean solution is higher than the oxysulfide content of lean solution, i.e. the ability that the energy force rate semi lean solution of lean solution absorption oxysulfide absorbs oxysulfide is strong.

In this manual, the main absorbent components in desulfuration solution, the composition that namely can absorb oxysulfide and oxysulfide is resolved can comprise at least a in organic alkali lye (for example, organic amine liquid) and various solion.In addition, desulfuration solution also comprises activator, acid and water.Selectively, desulfuration solution also can comprise anti-inefficacy agent, surfactant.

Renewable flue gas desulphurization process according to the present invention comprises by the absorption technique that absorbs the oxysulfide that contains in flue gas with desulfuration solution with by heating and comes desorb to be absorbed with the desulfuration solution of oxysulfide with the desorption technique of recovery oxysulfide.

Wherein, described absorption technique comprises the following steps of carrying out successively by the flow of flue gas direction: use the oxysulfide in the first desulfuration solution absorption flue gas, form the first rich solution; Use the second desulfuration solution further to absorb oxysulfide in flue gas, form the second rich solution, with the part of the second rich solution as the second desulfuration solution and with another part of the second rich solution as the first desulfuration solution, perhaps with the second whole rich solutions as the second desulfuration solution or as the first desulfuration solution; Use washing agent to capture the desulfuration solution of carrying secretly in flue gas; Discharge clean flue gas.Described desorption technique comprises the following steps: the part of the first rich solution is carried out a desorb, form semi lean solution and desorption gas; Simultaneously another part of the first rich solution and the part of semi lean solution are carried out the secondary desorb, form lean solution and desorption gas; Condensation is also reclaimed oxysulfide in desorption gas.Another part of semi lean solution as the first desulfuration solution, and is provided lean solution respectively to absorption technique as the second desulfuration solution, to realize the circulation of desulfuration solution between absorption technique and desorption technique; The oxysulfide content of described the first rich solution or the second rich solution is higher than the oxysulfide content of semi lean solution, and the oxysulfide content of described semi lean solution is higher than the oxysulfide content of lean solution.

In one embodiment of the invention, described renewable flue gas desulphurization process can comprise that also the oxysulfide content with the oxysulfide content of the second rich solution and semi lean solution compares, when the oxysulfide content of the second rich solution is higher, the second whole rich solutions is provided to described desorption technique together with the first rich solution.

In one embodiment of the invention, described absorption technique can comprise that also the use demister carries out the step of demist to described clean flue gas.

In one embodiment of the invention, in the capture step of described absorption technique, the trapping solution that contains desulfuration solution can be returned as cleaning solution and use.

In one embodiment of the invention, the capture step of described absorption technique also can comprise by trapping solution being carried out concentration or trapping solution is sent into the step that desorption system reclaims desulfuration solution together with rich solution.

In one embodiment of the invention, described cleaning solution can be industrial soft water, desalted water or a part of trapping solution.

In one embodiment of the invention, described desulfuration solution can be organic base solution, By Amine Solutions or can be low temperature absorption oxysulfide and at least a in the ionic liquid of desorption under high temperature oxysulfide.In addition, described desulfuration solution also can comprise activator, acid and water, perhaps also can comprise activator, acid, water and surfactant.

In one embodiment of the invention, the secondary desorb in described desorption technique can comprise by reboiler the first rich solution and/or second rich solution of part desorb carried out desorb.

In one embodiment of the invention, a desorb in described desorption technique can be the flash distillation desorb for HTHP desorb and secondary desorb, described HTHP desorb can realize by the first stripping stage that the bottom is provided with reboiler, described flash distillation desorb can realize by the second stripping stage that is connected with vacuum extractor, be provided with dividing plate between described the first stripping stage and the second stripping stage.

In one embodiment of the invention, described renewable flue gas desulphurization process washs flue gas before also can being included in and entering described absorption technique, so that flue gas is lowered the temperature and dedusting.Preferably, described washing step can realize through S shape flue and scrubbing tower successively by making pending flue gas, and wherein, described scrubbing tower can comprise void tower flue gas washing section, filler flue gas washing section and demist layer from the bottom up.In addition, described washing step can comprise that also the booster fan by being arranged on S shape flue front end makes the flue gas supercharging.

In one embodiment of the invention, described renewable flue gas desulphurization process also can comprise and carries out heat exchange to providing to the first rich solution of desorption technique and/or the second rich solution and lean solution and/or semi lean solution, with the temperature that improves the first rich solution and/or the second rich solution and reduce lean solution and/or the temperature of semi lean solution, thereby improved heating efficiency, and due to desulfuration solution at low temperatures (for example, 30 ℃~60 ℃) oxysulfide in flue gas is had better absorption efficiency, so the rear lean solution of purification heat and/or semi lean solution have also reached the temperature requirement of absorption technique.In addition, described renewable flue gas desulphurization process also can comprise first rich solution that will carry out a desorb and/or the second rich solution and desorption gas are carried out heat exchange, with the temperature of further raising the first rich solution and/or the second rich solution and reduce the temperature of desorption gas, thereby further improve heating efficiency.

In one embodiment of the invention, described renewable flue gas desulphurization process also can comprise to be processed providing to purify to recover to the lean solution of absorption technique, to remove suspension, metal cation and the strong acid radical ion that contains in lean solution.Wherein, described purification recovery treatment step can comprise sedimentation, filtration, freezing and crystallizing and the resin desalination step of carrying out in turn.Described purification recovery treatment step also can only comprise sedimentation, filtration and the freezing and crystallizing that carries out in turn, perhaps only comprises sedimentation, the filtration+resin desalination carried out in turn.In addition, described sedimentation and filtration step can carry out before lean solution is carried out heat exchange, and described freezing and crystallizing and resin desalination step can be carried out after lean solution is carried out heat exchange.In the present invention, described strong acid radical ion can comprise sulfate ion, chlorion and nitrate ion.In addition, described precipitation step also can comprise the step that adds precipitation by metallic ion agent and suspension filter aid in the lean solution for the treatment of sedimentation.In addition, described purification recovery treatment step also can comprise to adding alkali through sedimentation with filtering in the clear liquid that obtains, with the metal ion in further removal clear liquid.

In one embodiment of the invention, can carry out the purification recovery identical with foregoing to lean solution and semi lean solution respectively simultaneously processes.Namely, in one embodiment of the invention, described renewable flue gas desulphurization process also can comprise and purifies respectively recovery to the lean solution of absorption technique and semi lean solution and process providing, described purification recovery treatment step comprises sedimentation, filtration, freezing and crystallizing and the resin desalination step of carrying out in turn, thereby removes respectively suspension, metal cation and the strong acid radical ion that contains in lean solution and semi lean solution.In addition, described sedimentation and filtration step can carry out before lean solution or semi lean solution carry out heat exchange, and described freezing and crystallizing and resin desalination step can be carried out after lean solution or semi lean solution carry out heat exchange.

In one embodiment of the invention, described condensation and the step that reclaims the oxysulfide in desorption gas can comprise the following steps: desorption gas is carried out condensation to form condensate liquid and to carry the desorption gas of desulfuration solution secretly; The described desorption gas of carrying desulfuration solution secretly is carried out gas-liquid separation oxysulfide gas and liquid phase; Reclaim oxysulfide gas.Further, described condensation and the step that reclaims the oxysulfide in desorption gas also can comprise to condensate liquid with by the described liquid phase that gas-liquid separation obtains filters, and then filtrate is provided to a desorb or step that filtrate is effluxed.

In one embodiment of the invention, the described step that desorption gas is carried out condensation can comprise multi-stage condensing in sequence, and the condensate liquid that the first order condensation in described multi-stage condensing forms is discharged to the external world, the condensate liquid that other grade condensation in described multi-stage condensing forms through with the desorption gas heat exchange after provide to desorption technique.

In one embodiment of the invention, the described step that desorption gas is carried out condensation can comprise one-level condensation and B-grade condensation, the condensate liquid that described one-level condensation forms is discharged to the external world, the condensate liquid that described B-grade condensation forms through with the desorption gas heat exchange after provide to desorption technique.

Now, will describe exemplary embodiment of the present invention in detail.Example of the present invention illustrates in the accompanying drawings, and wherein, identical label represents identical element all the time.The below will describe embodiment by the reference accompanying drawing, to explain the present invention.Yet the present invention can implement with multiple different form, should not be understood to be confined to the exemplary embodiment in this proposition.It will be openly thorough with completely providing these embodiment to make of the present invention, and scope of the present invention is conveyed to those skilled in the art fully.In the accompanying drawings, for clarity, can exaggerate the layer and the zone size and relative size.

But here usage space relative terms (for example, " following ", " in ... below ", " top " etc.) describe as shown in FIG. element or the relative position relation of feature and other element or feature.It should be understood that the space relative terms is intended to comprise the different azimuth of device in using or operating except the orientation that is described in the drawings.For example, if device is reversed in the accompanying drawings, be described as other element or feature " following " or " " element of other element or feature " below " will be positioned as subsequently other element or feature " above " or " " element or the feature of other element or feature " top ".Therefore, exemplary term " following " can comprise top and following two kinds of orientation.

Describe below with reference to accompanying drawings renewable flue gas desulphurization process and system thereof according to an exemplary embodiment of the present invention in detail.

Embodiment 1

Figure 1A shows a kind of device schematic diagram for realizing the renewable flue gas desulphurization process of the first exemplary embodiment according to the present invention, and Figure 1B illustrates the renewable flue gas desulphurization process schematic diagram of the first exemplary embodiment according to the present invention.

As shown in Figure 1A, realize that the device of this exemplary embodiment can comprise: absorption system 100 contacts to absorb sulfur dioxide in flue gas by make lean solution and pending flue gas adverse current in the absorption tower, and forms rich solution and purified gas; Desorption system 200 makes the rich solution desorb to form new lean solution and desorption gas by desorber and reboiler; Desulfuration solution purifies resuscitation system 300, removes the foreign ion in the lean solution of desorb gained by the resin desalination; Desorption gas treatment system 600 uses the desorption gas condensation separator to obtain pure sulfur dioxide gas.

In realizing the device of this exemplary embodiment, the absorption tower of absorption system 100 comprises that flue gas passes through in turn and spaced semi lean solution absorber portion 110, lean solution absorber portion 120 and desulfuration solution captures section 130, semi lean solution absorber portion 110 is provided with semi lean solution entrance 111 and the first rich solution outlet 112, lean solution absorber portion 120 is provided with lean solution entrance 121 and the second rich solution outlet 122, and desulfuration solution captures section 130 and is provided with cleaning solution entrance 131 and trapping solution outlet 132.

In realizing the device of this exemplary embodiment, the desorber of desorption system 200 comprise spaced and the first stripping stage 210 of being communicated with below the first stripping stage and the second stripping stage 220 that is connected with reboiler 230, the first stripping stage 210 is provided with the first rich solution entrance 211 and semi lean solution outlet 212, the second stripping stages 220 are provided with the second rich solution entrance 221 and lean solution outlet 222.

In realizing the device of this exemplary embodiment, semi lean solution entrance 111 is connected with semi lean solution outlet 212 by the first pipeline 410 to use the semi lean solution that obtains from the first stripping stage 210 to come the sulfur dioxide in the absorption flue gas semi lean solution absorber portion 110; Lean solution entrance 121 is connected to use the next sulfur dioxide that absorbs in flue gas of lean solution that obtains from the second stripping stage 220 lean solution absorber portion 120 with lean solution outlet 222 by the second pipeline 420; The first rich solution outlet 112 is connected to provide rich solution to the first stripping stage 210 and the second stripping stage 220 by the 3rd pipeline 430 with the first rich solution entrance 211 with the second rich solution entrance 221; The second rich solution outlet 122 is connected with lean solution entrance 121 with semi lean solution entrance 111, recycle the part of the second rich solution is sent into semi lean solution absorber portion 110 and another part of the second rich solution is sent into lean solution absorber portion 120, in addition, the second rich solution outlet 122 also is connected with the 3rd pipeline 430, with when the content of sulfur dioxide in the second rich solution during higher than the content of sulfur dioxide in semi lean solution, the second whole rich solutions is sent into the 3rd pipeline then send into desorption system 200 and carry out desorb; Trapping solution outlet 132 is connected with cleaning solution entrance 131 by circulating pump 137, with realization, trapping solution is come the desulfuration solution of carrying secretly in the circularly trapping flue gas as cleaning solution; Be provided with the second poor rich liquid heat exchanger 413 between the first pipeline 410 and the 3rd pipeline 430; Be provided with the first poor rich liquid heat exchanger 412 between the second pipeline 420 and the 3rd pipeline 430.

In realizing the device of this exemplary embodiment, desulfuration solution purifies resuscitation system 300 and comprises sedimentation filtration system 310, freezing and crystallizing system 320 and the resin desalination system 330 of arranging in turn along the lean solution flow direction, desulfuration solution purifies resuscitation system 300 and is arranged on the second pipeline, and the first poor rich liquid heat exchanger 412 is arranged between sedimentation filtration system 310 and freezing and crystallizing system 320.

In realizing the device of this exemplary embodiment, be provided with desorption gas treatment system 600 above the first stripping stage 210.Described desorption gas treatment system 600 comprises: condenser, have desorption gas entrance, fog outlet and condensate outlet, and the desorption gas entrance is connected with the desorption gas outlet on the first stripping stage 210 tops, be used for the desorption gas that condensation is discharged from desorption technique, to form condensate liquid and fog, described fog is the desorption gas of carrying desulfuration solution secretly; Gas-liquid separator, have fog entrance, oxysulfide gas vent and discharge channel, and the fog entrance is connected with the fog outlet of condenser, be separated into oxysulfide gas (for example, sulfur dioxide gas and/or sulfur trioxide gas) and liquid phase for the desorption gas that will carry desulfuration solution secretly; Sulphur filter, have liquid inlet and filtrate (liquid, and liquid inlet and the condensate outlet of condenser are connected discharge channel and are connected with gas-liquid separator, top or filtrate (liquid that filtrate (liquid is connected to the first stripping stage 210 are connected to the external world, be used for filtering to condensate liquid with from the liquid phase that gas-liquid separator separates goes out, filter the filtrate that obtains and send into the first stripping stage 210 or the filtrate that filtration obtains is effluxed together with rich solution.

As shown in Figure 1B, the renewable flue gas desulphurization process of this exemplary embodiment can comprise absorption technique and the desorption technique that couples together by circulating of desulfuration solution.

Wherein, absorption technique comprises the following steps of carrying out successively by the flow of flue gas direction: the use semi lean solution absorbs the sulfur dioxide in flue gas in semi lean solution absorber portion 110, form the first rich solution; Use lean solution further sulfur dioxide that absorbs in flue gas in lean solution absorber portion 120, form the second rich solution, the part of the second rich solution is injected semi lean solution absorber portion 110 together with the semi lean solution that forms the first rich solution because of sulfur dioxide absorption, another part of the second rich solution is injected the lean solution absorber portion together with lean solution, during content of sulfur dioxide in the semi lean solution of discharging in higher than the first stripping stage 210 when the content of sulfur dioxide in the second rich solution, the second whole rich solutions is sent into desorption system 200 carry out desorb; Capture the desulfuration solution of carrying secretly in flue gas as washing agent with industrial pure water, and the trapping solution that capture is obtained is again as washing agent, circulation repeatedly, until after the desulfuration solution concentration in trapping solution reaches predetermined value, reclaim the desulfuration solution in trapping solution; Discharge clean flue gas.

Desorption technique comprises the following steps: the part to first rich solution of discharging from semi lean solution absorber portion 110 is carried out a desorb, forms semi lean solution and desorption gas; Simultaneously another part of the first rich solution and the part of semi lean solution are carried out the secondary desorb, form lean solution and desorption gas; Condensation is also reclaimed sulfur dioxide in desorption gas.

in this exemplary embodiment, renewable flue gas desulphurization process also can comprise: (1) to provide by the 3rd pipeline 430 to the first rich solution of desorption technique and/or the second rich solution (for example, the temperature of the first rich solution and/or the second rich solution is 45 ℃~55 ℃) with flow through the second pipeline 420 lean solution (for example, the temperature of lean solution is 95 ℃~120 ℃) carry out a heat exchange in the first poor rich liquid heat exchanger 412, thereby the temperature that improves the temperature of the first rich solution and/or the second rich solution and reduce lean solution (for example, after a heat exchange, the temperature of the first rich solution and/or the second rich solution is 65 ℃~80 ℃, the temperature of lean solution is 80 ℃~95 ℃), (2) to the first rich solution after a heat exchange and/or the second rich solution (for example, its temperature is 65 ℃~80 ℃) with the semi lean solution of discharging from the first stripping stage 210 (for example, its temperature is 95 ℃~110 ℃) carry out secondary heat exchange in the second poor rich liquid heat exchanger 413, temperature with further raising the first rich solution and/or the second rich solution, (for example reduce simultaneously the temperature of semi lean solution, the temperature of the first rich solution and/or the second rich solution is 80 ℃~95 ℃ after secondary heat exchange, and the temperature of semi lean solution is 85 ℃~95 ℃).

In addition, in this exemplary embodiment, in order further being reduced to below 60 ℃ through the lean solution of heat exchange or the temperature of semi lean solution, also can to carry out heat exchange again to lean solution and cooling water, also can to carry out heat exchange again to semi lean solution and cooling water.

In this exemplary embodiment, to provide through the part of the first rich solution after a heat exchange and/or the second rich solution to the second stripping stage 220 and directly carry out the secondary desorb, will all send into the first stripping stage 210 through the first rich solution after a heat exchange and secondary heat exchange and/or the second rich solution and carry out a desorb.But the invention is not restricted to this, for example, also can carry out a heat exchange and secondary heat exchange to the first whole rich solutions and/or the second rich solution, and will send into the second stripping stage 220 through the part of the first rich solution after heat exchange and/or the second rich solution and carry out the secondary desorb, another part is sent into the first stripping stage 210 and is carried out a desorb.

In this exemplary embodiment, renewable flue gas desulphurization process also comprises the step that the lean solution after resolving is purified recovery.Specifically, export 222 through the lean solution of secondary desorb by lean solution and enter the second pipeline 420 in the second stripping stage 220, then sedimentation filtration system 310, the freezing and crystallizing system 320, resin desalination system 330 and the lean solution entrance 121 that purify resuscitation system 300 by desulfuration solution in turn enter the lean solution absorber portion 120 on absorption tower, thereby realize recycling of desulfuration solution.Here, lean solution is carried out heat exchange at First Heat Exchanger 412 places between sedimentation filtration system 310 and freezing and crystallizing system 320 and the rich solution in the 3rd pipeline 430, so that lean solution is lowered the temperature and rich solution is heated up.Sedimentation filtration system 310 is by adding precipitation by metallic ion agent and suspension filter aid in lean solution, remove in lean solution suspension (for example, dust etc.) and/or metal ion, and can reduce the sedimentation of suspension in First Heat Exchanger 412 or the second pipeline 420 after it, reduce the obstruction of the second pipeline 420.Freezing and crystallizing system 320 is by carrying out basicity and regulate and the operation such as cooling removing and reclaim sulfate radical plasma (SO in lean solution to lean solution 2- 4), thereby reduced the load of resin desalination system 320.Resin desalination system 330 is used for removing the chlorion (Cl of lean solution -), nitrate ion (NO - 3) and sulfate radical (SO 2- 4) etc. the strong acid radical ion.

In this exemplary embodiment, renewable flue gas desulphurization process comprises that also the desorption gas that desorption technique is obtained carries out condensation and reclaims the step of oxysulfide.Described condensation and the step that reclaims the oxysulfide in desorption gas comprise the following steps: desorption gas is carried out condensation to form condensate liquid and to carry the desorption gas of desulfuration solution secretly; The described desorption gas of carrying desulfuration solution secretly is carried out gas-liquid separation oxysulfide gas and liquid phase; Reclaim oxysulfide gas.In addition, described condensation and the step that reclaims the oxysulfide in desorption gas also can comprise to condensate liquid with by the described liquid phase that gas-liquid separation obtains filters, and then filtrate is provided to a desorb or step that filtrate is effluxed.Described condensing steps is realized by condenser.Described gas-liquid separation realizes by gas-liquid separator.Described filtration realizes by sulphur filter.

Embodiment 2

Fig. 2 A shows a kind of device schematic diagram for realizing the renewable flue gas desulphurization process of the second exemplary embodiment according to the present invention, and Fig. 2 B illustrates the renewable flue gas desulphurization process schematic diagram of the second exemplary embodiment according to the present invention.

As shown in Fig. 2 A, realize the device of this exemplary embodiment and realize that the difference of the device of embodiment 1 is following content:

(1) device of realizing this exemplary embodiment comprises washing system 500.Before flue gas washing system 500 is arranged on absorption system, be used for the flue gas that contains sulfur dioxide that washing is about to enter absorption system 100, to remove the impurity such as dust that contain in flue gas.In addition, for the higher situation of pending flue-gas temperature (for example, pending flue gas is metallurgy sintering smoke), washing system 500 can be reduced to the temperature of flue gas the temperature (for example, 30 ℃~60 ℃) that is suitable for absorbing with desulfuration solution oxysulfide wherein.Certainly, when not too being fit to if the temperature of pending flue gas is lower absorb wherein oxysulfide with desulfuration solution, also can be by washing system 500 use hot water with the adjustment of pending flue gas to the temperature (for example, 30 ℃~60 ℃) that is suitable for absorbing with desulfuration solution oxysulfide wherein.Here, when the desulfuration solution composition not simultaneously, its temperature that is suitable for absorbing oxysulfide also may be different.

(2) in realizing the device of this exemplary embodiment, the first flue gas that semi lean solution absorber portion 110 can comprise the first rich solution groove 116 and have each other the first preset distance rises gas hood 113 and first liquid distributor 115, and first liquid distributor 115 is communicated with semi lean solution entrance 111 and the first rich solution groove 116 is communicated with the first rich solution outlet 112.Here, the first preset distance is used for by increasing the mode of flue gas range ability, make the abundant sedimentation of dust in flue gas, and the first preset distance can be used for and will extremely be fit to the temperature of sulfur dioxide absorption through the temperature that semi lean solution and the abundant counter current contacting of flue gas of 115 distributions of first liquid distributor are regulated flue gas.In addition, when the first flue gas rose gas hood 113 or first liquid distributor 115 and needs repairing, the first preset distance can facilitate the staff to enter semi lean solution absorber portion 110 they are keeped in repair.In addition, alternatively, rise between gas hood 113 and first liquid distributor 115 at first flue gas of the present embodiment and can also be provided with the first packing layer 114, and the distance that the first packing layer 114 and the first flue gas rise between gas hood 113 is the first preset distance, thereby can make the abundant sedimentation of dust in flue gas, can make again flue gas and semi lean solution carry out counter current contacting more fully.

(3) in realizing the device of this exemplary embodiment, lean solution absorber portion 120 comprises that the second flue gas that has each other the second preset distance rises gas hood 123, the second packing layer 124, second liquid distributor 125 and the second rich solution groove 126, and the second liquid distributor is communicated with the lean solution entrance and the second rich solution groove is communicated with the second rich solution outlet.Desulfuration solution captures section 130 and comprises that the 3rd flue gas that has each other the second preset distance rises gas hood 133, the 3rd packing layer 134, the 3rd liquid distribution trough 135 and captures liquid bath 136, the three liquid distribution troughs 135 and be communicated with cleaning solution entrance 131 and capture liquid bath 136 and export 132 with trapping solution and be communicated with.In addition, flue gas demist layer 140 can be arranged on place, top, absorption tower, and between the 3rd liquid distribution trough 135 of clean gas outlet and flue gas trapping section 130.Flue gas demist layer 140 can comprise two-layer demister, and has preset distance between this two-layer demister.In the present invention, entering from cleaning solution entrance 131 cleaning solution that desulfuration solution captures section 130 is industrial soft water, desalted water or a part of trapping solution.

(4) in realizing the device of this exemplary embodiment, the bottom of the first stripping stage 210 arranges the second reboiler 230 ' to realize that the rich solution that enters the first stripping stage 210 is carried out the HTHP desorb; The second stripping stage 220 does not arrange reboiler, and the top of the second stripping stage 220 is connected with the vacuum extractor (not shown) to realize that the rich solution that enters the second stripping stage 220 is carried out the flash distillation desorb, the desorption gas of extracting out by vacuum extractor can provide to desorption gas treatment system 600, and is provided with dividing plate 250 between described the first stripping stage 210 and the second stripping stage 220.

(5) in realizing the device of this exemplary embodiment, the first stripping stage 210 comprises that the first desorption gas that has each other the second preset distance rises gas hood 213, the 4th packing layer 214, the 4th liquid distribution trough 215 and semi lean solution storage tank 216, and semi lean solution storage tank 216 is communicated with semi lean solution outlet 212; The second stripping stage 220 comprises that the second desorption gas that has each other the second preset distance rises gas hood 223, the 5th packing layer 224, the 5th liquid distribution trough 225 and lean solution storage tank 226, and lean solution storage tank 226 is communicated with lean solution outlet 222.In addition, desorber demist layer 240 can be arranged on place, desorber top and between the 4th liquid distribution trough 215 of desorption gas outlet and the first stripping stage 210.Desorber demist layer 240 can comprise two-layer demister, and has preset distance between this two-layer demister.

(6) in realizing the device of this exemplary embodiment, the rich solution that obtains by the absorption tower transports by the 3rd pipeline 430, and through after the first poor rich liquid heat exchanger 412 and the second poor rich liquid heat exchanger 413 heat exchange, enter the first stripping stage 210 and the second stripping stage 220 by the first rich solution entrance 211 and the second rich solution entrance 221 respectively successively.

In realizing device of the present invention, described filler can be various structured packings or dumped packing.For example, plastics deflection plate filler, ripple deflection plate with holes, metallurgic orifice corrugated packing, plastic filler in bulk, ball-type dumped packing etc.In realizing device of the present invention, demister can be electrostatic precipitator, deflection plate demister or mesh mist eliminator.In realizing device of the present invention, it is in order to facilitate the staff that each equipment is keeped in repair that the second preset distance is set.In realizing device of the present invention, absorption tower and desorber inside such as liquid distribution trough, rise between the neighbouring device of gas hood, packing layer, demister etc. and all can have the second preset distance, with convenient for maintaining.In realizing device of the present invention, can setting and the industrial clean water system of the equipment connection such as liquid distribution trough, packing layer, demister, to realize the cleaning to equipment such as liquid distribution trough, packing layer, demisters, for example, also can come the equipment such as cleaning liquid distributor, packing layer, demister by injecting industrial clean water from the liquid inlet of each section of each section on absorption tower or desorber.

In realizing device of the present invention, the purpose that rises gas hood, packing layer, liquid distribution trough etc. is set in the absorption tower is to make flue gas and desulfuration solution to carry out counter current contacting fully, thereby improve desulfuration solution to the absorptivity of sulfur dioxide; The purpose that rises gas hood, packing layer, liquid distribution trough is set in desorber is to extend the time of staying of rich solution in desorber, so that the abundant desorb of rich solution, and make the gas of rich solution and reboiler generation carry out counter current contacting, rich solution is heated and improves desorption effect; The effect that demister is set is to remove desulfuration solution or the moisture in flue gas or desorption gas.Therefore, although described in this exemplary embodiment to be provided with in absorption tower and desorber and risen gas hood, packing layer, liquid distribution trough, demister etc., but those skilled in the art should understand that to the invention is not restricted to this, and can realize rising by other similar devices equipment roles in realizing device of the present invention such as gas hood, packing layer, liquid distribution trough, demister.

As shown in Fig. 2 B, the renewable flue gas desulphurization process of this exemplary embodiment can comprise absorption technique and the desorption technique that couples together by circulating of desulfuration solution.

Specifically, the renewable flue gas desulphurization process of this exemplary embodiment comprises following content:

At first, treat smoke treatment and wash, so that it is lowered the temperature and dedusting.Preferably, described washing step can realize through S shape flue and scrubbing tower successively by making pending flue gas, and wherein, described scrubbing tower can comprise void tower flue gas washing section, filler flue gas washing section and demist layer from the bottom up.In addition, described washing step can comprise that also the booster fan by being arranged on S shape flue front end makes the flue gas supercharging.

Then, absorb oxysulfide in flue gas by absorption technique, and remove simultaneously impurity such as dust, heavy metal element and oxysulfide in flue gas to realize the purification to flue gas.Described absorption technique comprises the following steps of carrying out successively by the flow of flue gas direction: the use semi lean solution absorbs the sulfur dioxide in flue gas in semi lean solution absorber portion 110, form the first rich solution; Use lean solution further sulfur dioxide that absorbs in flue gas in lean solution absorber portion 120, form the second rich solution, the part of the second rich solution is injected semi lean solution absorber portion 110 together with the semi lean solution that forms the first rich solution because of sulfur dioxide absorption, another part of the second rich solution is injected the lean solution absorber portion together with lean solution, during content of sulfur dioxide in the semi lean solution of discharging in higher than the first stripping stage 210 when the content of sulfur dioxide in the second rich solution, the second whole rich solutions is sent into semi lean solution absorber portion 210; Capture the desulfuration solution of carrying secretly in flue gas as washing agent with industrial pure water, and the trapping solution that capture is obtained is again as washing agent, circulation repeatedly, until after the desulfuration solution concentration in trapping solution reaches predetermined value, reclaim the desulfuration solution in trapping solution; Flue gas is carried out demist to be processed; Discharge clean flue gas.

Next, the rich solution that absorption technique is obtained carries out desorb, obtains lean solution, semi lean solution and desorption gas, and desorption gas is carried out condensation, filtration treatment, thereby obtains pure oxysulfide.Described desorption technique comprises the following steps: the part to first rich solution of discharging from semi lean solution absorber portion 110 is carried out the HTHP desorb, forms semi lean solution and desorption gas; Simultaneously another part of the first rich solution and the part of semi lean solution are carried out the flash distillation desorb, form lean solution and desorption gas; Condensation is also reclaimed oxysulfide in desorption gas.

In this exemplary embodiment, renewable flue gas desulphurization process also can comprise: (1) carries out a heat exchange to providing by the 3rd pipeline 430 to the first rich solution of desorption technique and the lean solution of second pipeline 420 of flowing through in the first poor rich liquid heat exchanger 412, thereby improves the temperature of the first rich solution and reduce the temperature of lean solution; (2) to carrying out secondary heat exchange through the first rich solution after a heat exchange and the semi lean solution of discharging from the first stripping stage 210 the second poor rich liquid heat exchanger 413, with the temperature of further raising the first rich solution, reduce simultaneously the temperature of semi lean solution.

In this exemplary embodiment, the the first whole rich solution that obtains from absorption technique is carried out a heat exchange and secondary heat exchange, and will send into the second stripping stage 220 through the part of the first rich solution after heat exchange and carry out the HTHP desorb, another part is sent into the first stripping stage 210 and is carried out the flash distillation desorb.

The technique of this exemplary embodiment also comprises the step that the lean solution after resolving is purified recovery.Specifically, export 222 through the lean solution of flash distillation desorb by lean solution and enter the second pipeline 420 in the second stripping stage 220, then sedimentation filtration system 310, the freezing and crystallizing system 320, resin desalination system 330 and the lean solution entrance 121 that purify resuscitation system 300 by desulfuration solution in turn enter the lean solution absorber portion 120 on absorption tower, thereby realize recycling of desulfuration solution.Here, lean solution is carried out heat exchange at First Heat Exchanger 412 places between sedimentation filtration system 310 and freezing and crystallizing system 320 and the rich solution in the 3rd pipeline 430, so that lean solution is lowered the temperature and rich solution is heated up.Sedimentation filtration system 310 is by adding precipitation by metallic ion agent and suspension filter aid in lean solution, remove in lean solution suspension (for example, dust etc.) and/or metal ion, and can reduce the sedimentation of suspension in First Heat Exchanger 412 or the second pipeline 420 after it, reduce the obstruction of the second pipeline 420.Freezing and crystallizing system 320 is by carrying out basicity and regulate and the operation such as cooling removing and reclaim sulfate radical plasma (SO in lean solution to lean solution 2- 4), thereby reduced the load of resin desalination system 320.Resin desalination system 330 is used for removing the chlorion (Cl of lean solution -), nitrate ion (NO - 3) and sulfate radical (SO 2- 4) etc. the strong acid radical ion.

In addition, renewable flue gas desulphurization process of the present invention also can be included in the step that the front rich solution that absorption technique is obtained of a heat exchange cushions, and provides to the flowing velocity of the rich solution of desorption technique with storage rich solution and adjusting, thereby regulates rhythm of production.Here, the described step that rich solution is cushioned can realize by between first rich solution outlet the 112 and first poor rich liquid heat exchanger 412 of semi lean solution absorber portion 110, rich solution dashpot (not shown) being set.

In addition, renewable flue gas desulphurization process of the present invention also can be included in the step that the front rich solution that absorption technique is obtained of a heat exchange filters, removing the impurity such as suspension and dust in rich solution, thereby help long-term, the effectively direct motion of renewable flue gas desulphurization process of the present invention.The described step that rich solution is filtered can realize by between first rich solution outlet the 112 and first poor rich liquid heat exchanger 412 of semi lean solution absorber portion 110, the first rich solution filter (not shown) being set.Preferably, the described step that rich solution is filtered can be carried out before the described step that rich solution is cushioned.

In addition, renewable flue gas desulphurization process of the present invention also can comprise will provide to what obtain after a desorb the step that purifies the recovery processing to the semi lean solution of semi lean solution absorber portion, to remove suspension, metal cation and the strong acid radical ion that contains in semi lean solution.Wherein, describedly semi lean solution is purified the recovery treatment step can comprise sedimentation, filtration, freezing and crystallizing and the resin desalination step of carrying out in turn.In addition, described sedimentation and filtration step can carry out before semi lean solution carries out heat exchange, and described freezing and crystallizing and resin desalination step can be carried out after semi lean solution carries out heat exchange.In the present invention, described strong acid radical ion can comprise sulfate ion, chlorion and nitrate ion.In addition, described precipitation step also can comprise the step that adds precipitation by metallic ion agent and suspension filter aid in the lean solution for the treatment of sedimentation.In addition, described purification recovery treatment step also can comprise to adding alkali through sedimentation with filtering in the clear liquid that obtains, with the metal ion in further removal clear liquid.Here, describedly semi lean solution is purified step that recovery processes can purify the resuscitation system (not shown) and realize by the second desulfuration solution is set in the first pipeline 410.The structure of described the second desulfuration solution purification resuscitation system and desulfuration solution purification resuscitation system 300 is basic identical, difference is: the second desulfuration solution purifies resuscitation system and is arranged on the first pipeline 410, and comprise the second sedimentation filtration system (not shown), second freezing and crystallizing system's (not shown) and the second resin desalination system (not shown) of arranging in turn along the semi lean solution flow direction, and the second poor rich liquid heat exchanger 413 is between the second sedimentation filtration system and the second freezing and crystallizing system.

In realizing the device of flue gas desulfurization technique of the present invention, described sedimentation filtration system (310) or the second sedimentation filtration system can comprise subsider and the filter of serial connection successively, what described freezing and crystallizing system (320) or the second freezing and crystallizing system can comprise serial connection successively adds alkali groove, freezing and crystallizing device, centrifugal separator and freezing and crystallizing underground tank, and described resin desalination system (330) or the second resin desalination system can comprise active carbon adsorption groove, resin adsorption groove and the solution tank of serial connection successively.In addition, described sedimentation filtration system (310) also comprises the precipitating reagent make-up tank that is connected with described subsider.In addition, described subsider also is directly connected to the described alkali groove that adds.Owing to being provided with the precipitating reagent make-up tank that is connected with subsider, so described precipitation step also can comprise the step that adds precipitation by metallic ion agent and suspension filter aid in the lean solution for the treatment of sedimentation.

Specifically, the step that in the present invention, desulfuration solution is purified recovery can realize by the following method:

(1) make suspension, metal cation precipitation: adopt self-cleaning recoil lean solution filter, lean solution or semi lean solution are filtered, add filter aid, metal-precipitator, solution adopts sheet frame to carry out press filtration, remove the suspension particle diameter greater than suspension and the precipitation by metallic ion thing of 50um, after press filtration, solution is sent into except carbon filter, in order to remove organic acid ion and desulfuration solution degradation material in a small amount.Solution after de-carbon further carries out mechanical filter.Remove the suspension particle diameter greater than suspended sediment and the activated carbon particles of 5um.Wherein filter aid is one or both of silica containing diatomite or diatomite and sial filter aid, and metal-precipitator is inorganic alkaline thing and organic substance, and inorganic base substance is mainly NaOH, KOH, NaH 2PO 4, Na 2HPO 4, K 2HPO 4, KH 2PO 4, the organic matter precipitating reagent is sodium diethyldithiocarbamate.

(2) freezing and crystallizing is to remove sulfate radical: regulate with the lean solution that is removed metal ion or the basicity of semi lean solution, form the first mixing material, the first further decrease temperature crystalline of mixing material is the second mixing material, and separates out a sodium sulphate shape crystal.

(3) resin removes the strong acid radical ions such as chlorine root, nitrate anion, to send into resin bed with the lean solution that is removed metal ion or semi lean solution or the second mixing material, so that need the liquid of resin treatment flow through from the top down resin bed or the resin bed of flowing through from bottom to top, form the 3rd mixing material through the solution of purified treatment.In the resin washing process, can arrange increases the air blow drying operation, reduces resin to the adsorbance of desulfuration solution.Loss when reducing the resin alkali cleaning.

In addition, in another exemplary embodiment of the present invention, the described step that desorption gas is carried out condensation can comprise multi-stage condensing in sequence, and the condensate liquid that the first order condensation in described multi-stage condensing forms is discharged to the external world, the condensate liquid that other grade condensation in described multi-stage condensing forms through with the desorption gas heat exchange after provide to desorption technique.For example, the described step that desorption gas is carried out condensation can comprise one-level condensation and B-grade condensation, and the condensate liquid that described one-level condensation forms is discharged to the external world, the condensate liquid that described B-grade condensation forms through with the desorption gas heat exchange after provide to desorption technique.The present embodiment can be realized by the desorption gas treatment system 600 in embodiment 1 is set to following structure.In described desorption gas treatment system, condenser can be comprised of first-stage condenser and secondary condenser.Wherein, first-stage condenser has desorption gas entrance, the first fog outlet and the first condensate outlet, and the desorption gas entrance exports with the desorption gas on the first stripping stage 210 tops and be connected, and the one-level condensate outlet is connected to the external world; Secondary condenser has the first fog entrance, the second fog outlet and the second condensate outlet, the first fog entrance is connected with the first fog outlet, the second condensate outlet is connected with the liquid inlet of sulphur filter, the second fog outlet is connected with the fog entrance of gas-liquid separator, and the filtrate (liquid of described sulphur filter is connected to the top of the first stripping stage 210.The 3rd heat exchanger is set between the top of described filtrate (liquid and the first stripping stage 210, and the 3rd heat exchanger is between desorption gas outlet and condenser, thereby can realize the heat exchange to filtrate and desorption under high temperature gas, so that the temperature of desorption under high temperature gas is reduced and improves the temperature of the filtrate that is about to enter the first stripping stage.

The above-mentioned step that desorption gas is carried out multi-stage condensing has the following advantages.The below take condensed in two stages as example illustrates above-mentioned advantage.(for example, can be 80~95 ℃ through the condensed acid gas of one-level (that is, through condensed desorption gas) temperature, condensate temperature can be 80~95 ℃ to the temperature that the temperature of the condensate liquid that usually, obtains due to the one-level condensation obtains higher than B-grade condensation; Acid gas temperature after B-grade condensation can be 55~65 ℃, condensate temperature can be 50~65 ℃), so the condensate liquid that first-stage condenser obtains contains water, a small amount of sulfurous acid, and the condensate liquid that secondary condenser obtains contains a small amount of desulfurizing agent, water, saturated sulfurous acid.The condensate liquid that first-stage condenser is obtained effluxes, and can avoid causing the concentration of the desulfuration solution in flue gas desulphurization system too low owing to introducing the moisture that contains in cleaning solution or industrial pure water or flue gas in flue gas desulphurization system; And the condensate liquid that secondary condenser obtains is returned to desorption system, and can reduce the loss of desulfurizing agent in desulfuration solution, improve the rate of recovery of oxysulfide, and avoid the reduction of the desulfuration solution concentration in flue gas desulphurization system.Although the above has specifically described the situation of desorption gas being carried out condensed in two stages, it should be appreciated by those skilled in the art that in the present invention the step that desorption gas is carried out condensation also can comprise in sequence three grades of condensations or condensation more than three grades.

Although the above has described renewable flue gas desulphurization process of the present invention in conjunction with some exemplary embodiments, but those skilled in the art should be clear, in the situation that do not break away from the spirit and scope that claim limits, can modify and change above-mentioned exemplary embodiment.

Claims (27)

1. renewable flue gas desulphurization process, it is characterized in that, described renewable flue gas desulphurization process comprises by the absorption technique that absorbs the oxysulfide that contains in flue gas with desulfuration solution with by heating and comes desorb to be absorbed with the desulfuration solution of oxysulfide with the desorption technique of recovery oxysulfide, wherein
Described absorption technique comprises the following steps of carrying out successively by the flow of flue gas direction: use the oxysulfide in the first desulfuration solution absorption flue gas, form the first rich solution; Use the second desulfuration solution further to absorb oxysulfide in flue gas, form the second rich solution, with the second rich solution as the second desulfuration solution or as the first desulfuration solution; Use washing agent to capture the desulfuration solution of carrying secretly in flue gas; Discharge clean flue gas;
Described desorption technique comprises the following steps: the part of the first rich solution is carried out a desorb, form semi lean solution and desorption gas; Simultaneously another part of the first rich solution and the part of semi lean solution are carried out the secondary desorb, form lean solution and desorption gas; Condensation is also reclaimed oxysulfide in desorption gas;
Another part of semi lean solution as the first desulfuration solution, and is provided lean solution respectively to absorption technique as the second desulfuration solution;
The oxysulfide content of described the first rich solution or the second rich solution is higher than the oxysulfide content of semi lean solution, and the oxysulfide content of described semi lean solution is higher than the oxysulfide content of lean solution.
2. renewable flue gas desulphurization process as claimed in claim 1, it is characterized in that, described renewable flue gas desulphurization process comprises that also the oxysulfide content with the oxysulfide content of the second rich solution and semi lean solution compares, when the oxysulfide content of the second rich solution is higher, the second rich solution is provided to described desorption technique together with the first rich solution.
3. renewable flue gas desulphurization process as claimed in claim 1, is characterized in that, described absorption technique comprises that also the use demister carries out the step of demist to described clean flue gas.
4. renewable flue gas desulphurization process as claimed in claim 1, is characterized in that, in the capture step of described absorption technique, the trapping solution that will contain desulfuration solution returns as cleaning solution and uses.
5. renewable flue gas desulphurization process as claimed in claim 1, is characterized in that, the capture step of described absorption technique also comprises by trapping solution being carried out concentration or trapping solution is sent into the step that desorption system reclaims desulfuration solution together with rich solution.
6. renewable flue gas desulphurization process as claimed in claim 1, is characterized in that, described washing agent is industrial soft water, desalted water or a part of trapping solution.
7. renewable flue gas desulphurization process as claimed in claim 1, is characterized in that, described desulfuration solution is at least a in organic base solution or ionic liquid.
8. renewable flue gas desulphurization process as claimed in claim 7, is characterized in that, described desulfuration solution also comprises activator, acid and water.
9. renewable flue gas desulphurization process as claimed in claim 1, is characterized in that, the secondary desorb in described desorption technique comprises by reboiler carries out desorb to the first rich solution and/or second rich solution of part desorb.
10. renewable flue gas desulphurization process as claimed in claim 1, it is characterized in that, a desorb in described desorption technique is that HTHP desorb and secondary desorb are the flash distillation desorb, described HTHP desorb realizes by the first stripping stage that the bottom is provided with reboiler, described flash distillation desorb realizes by the second stripping stage that is connected with vacuum extractor, is provided with dividing plate between described the first stripping stage and the second stripping stage.
11. renewable flue gas desulphurization process as described in any one in claim 1 to 10 is characterized in that, described renewable flue gas desulphurization process washs flue gas before also being included in and entering described absorption technique, so that flue gas is lowered the temperature and dedusting.
12. renewable flue gas desulphurization process as claimed in claim 11, it is characterized in that, described washing step is by realizing successively pending flue gas through S shape flue and scrubbing tower, wherein, described scrubbing tower comprises void tower flue gas washing section, filler flue gas washing section and demist layer from the bottom up.
13. renewable flue gas desulphurization process according to claim 11 is characterized in that, described washing step comprises that also the booster fan by being arranged on S shape flue front end makes the flue gas supercharging.
14. renewable flue gas desulphurization process as described in any one in claim 1 to 10, it is characterized in that, described renewable flue gas desulphurization process also comprises and carries out heat exchange to providing to the first rich solution of desorption technique and/or the second rich solution and lean solution and/or semi lean solution, with the temperature that improves the first rich solution and/or the second rich solution and reduce lean solution and/or the temperature of semi lean solution.
15. renewable flue gas desulphurization process as claimed in claim 14, it is characterized in that, described renewable flue gas desulphurization process also comprises first rich solution that will carry out a desorb and/or the second rich solution and desorption gas carried out heat exchange, with the temperature of further raising the first rich solution and/or the second rich solution and reduce the temperature of desorption gas.
16. renewable flue gas desulphurization process as claimed in claim 14 is characterized in that, before described renewable flue gas desulphurization process also is included in described heat exchange, and the step that the first rich solution of obtaining from described absorption technique and/or the second rich solution are cushioned.
17. renewable flue gas desulphurization process as claimed in claim 14 is characterized in that, before described renewable flue gas desulphurization process also is included in described heat exchange, and the step that the first rich solution of obtaining from described absorption technique and/or the second rich solution are filtered.
18. renewable flue gas desulphurization process as described in any one in claim 1 to 10, it is characterized in that, described renewable flue gas desulphurization process also comprises to be processed providing to purify to recover to the lean solution of absorption technique, removing suspension, metal cation and the strong acid radical ion that contains in lean solution, described purification recovery treatment step comprises in sedimentation, filtration, freezing and crystallizing and the resin desalination step of carrying out in turn front at least two.
19. renewable flue gas desulphurization process as claimed in claim 18, it is characterized in that, described renewable flue gas desulphurization process also comprises to be processed providing to purify to recover to the semi lean solution of absorption technique, removing suspension, metal cation and the strong acid radical ion that contains in semi lean solution, described purification recovery treatment step comprises in sedimentation, filtration, freezing and crystallizing and the resin desalination step of carrying out in turn front at least two.
20. renewable flue gas desulphurization process as claimed in claim 18 is characterized in that, described sedimentation and filtration step carry out before rich solution and lean solution are carried out heat exchange.
21. renewable flue gas desulphurization process as claimed in claim 18 is characterized in that, described strong acid radical ion comprises sulfate ion, chlorion and nitrate ion.
22. renewable flue gas desulphurization process as claimed in claim 18 is characterized in that, described precipitation step also comprises the step that adds precipitation by metallic ion agent and suspension filter aid in the lean solution for the treatment of sedimentation.
23. renewable flue gas desulphurization process as claimed in claim 18 is characterized in that, described purification recovery treatment step also comprises to adding alkali through sedimentation with filtering in the clear liquid that obtains, with the metal ion in further removal clear liquid.
24. renewable flue gas desulphurization process as described in any one in claim 1 to 10, it is characterized in that, described condensation and the step that reclaims the oxysulfide in desorption gas comprise the following steps: desorption gas is carried out condensation to form condensate liquid and to carry the desorption gas of desulfuration solution secretly; The described desorption gas of carrying desulfuration solution secretly is carried out gas-liquid separation oxysulfide gas and liquid phase; Reclaim oxysulfide gas.
25. renewable flue gas desulphurization process as claimed in claim 24, it is characterized in that, described condensation and the step that reclaims the oxysulfide in desorption gas also comprise to condensate liquid with by the described liquid phase that gas-liquid separation obtains filters, then will provide to the step of a desorb after filtrate and desorption gas heat exchange, perhaps described condensation and the step that reclaims the oxysulfide in desorption gas also comprise to condensate liquid with by the described liquid phase that gas-liquid separation obtains and filtering.
26. renewable flue gas desulphurization process as claimed in claim 24, it is characterized in that, the described step that desorption gas is carried out condensation comprises multi-stage condensing in sequence, and the condensate liquid that the first order condensation in described multi-stage condensing forms is discharged to the external world, the condensate liquid that other grade condensation in described multi-stage condensing forms through with the desorption gas heat exchange after provide to desorption technique.
27. renewable flue gas desulphurization process as claimed in claim 24, it is characterized in that, the described step that desorption gas is carried out condensation comprises one-level condensation and B-grade condensation, the condensate liquid that described one-level condensation forms is discharged to the external world, the condensate liquid that described B-grade condensation forms through with the desorption gas heat exchange after provide to desorption technique.
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CN105056711B (en) * 2015-08-21 2017-05-31 马鞍山艺诚机电有限公司 SO in flue gas2The nested citrate technique for absorbing parsing of multistage of purification
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