CN107335322A - One kind is from containing SO2Recovering liquid SO in flue gas2Technique - Google Patents
One kind is from containing SO2Recovering liquid SO in flue gas2Technique Download PDFInfo
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- CN107335322A CN107335322A CN201611026242.3A CN201611026242A CN107335322A CN 107335322 A CN107335322 A CN 107335322A CN 201611026242 A CN201611026242 A CN 201611026242A CN 107335322 A CN107335322 A CN 107335322A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/02—Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/48—Sulfur dioxide; Sulfurous acid
- C01B17/50—Preparation of sulfur dioxide
- C01B17/56—Separation; Purification
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/20—Organic adsorbents
- B01D2253/202—Polymeric adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses one kind from containing SO2Recovering liquid SO in flue gas2Technique, comprise the following steps：(1) SO will be contained2Flue gas through poor sulfur absorbing agent absorption cleaning, the flue gas emptying after purification, absorb SO2The poor sulfur absorbing agent become sulfur-rich absorbent, then to the SO in the sulfur-rich absorbent by the way of air air lift2Desorbed；(2) desorption SO in recycling step (1)2The sulfur-rich absorbent afterwards is as the poor sulfur absorbing agent in the step (1) absorbing the SO in flue gas2, desorption caused by be rich in SO2Stripping gas it is compressed, condensation obtain liquid SO2；Wherein, the absorbent is NHD.Above-mentioned technique overcomes the defects of technique desulfuration efficiency that sulfur dioxide is reclaimed in flue gas of the prior art is low, product purity is low, high energy consumption and cost are high.
Description
Technical field
The invention belongs to flue gas desulfurization field, and in particular to one kind is from containing SO2Recovering liquid SO in flue gas2Technique.
Background technology
SO2SO can be oxidized in an atmosphere3, be dissolved in steam formation secondary pollution sulfuric acid mist, to respiratory tract attachment and
Stimulation is stronger, if sulfuric acid mist condenses into bulky grain, declines form acid rain to the cold.Based on meteorological condition in 2010, entirely
State SO2, NOx, a PM 2.5 and NH3Environmental carrying capacity estimated value respectively may be about 13,600,000 tons, 12,600,000 tons, 6,200,000 tons and
6300000 tons；And national SO in 20102Actual emission exceedes the 66% of its environmental carrying capacity estimated value respectively, exceeds well over big compression ring
Border capacity.The SO wherein discharged in the flue gas of industrial discharge2Account for SO2Total release proportion is larger, in order to reduce SO2Discharge capacity, more
It is directed to studying the sulfur removal technology of flue gas come more countries, to reduce the SO in flue gas2Discharged into air.
From the 1950s, the multinational desulfurization technology that just begins one's study in the world, desulfurization technology is up to hundreds of so far.Pass
The flue gas desulfurization technique of system mainly has limestone/gypsum method, sodium alkali, zinc oxide method, sour method etc..Such as limestone/gypsum method,
This method key step is as follows：Flue gas flows upwardly through spray section after entering in tower, in a counter-current configuration the lime stone with spraying
Slurry liquid contacts, the SO in flue gas2Concurrent biochemical reaction is absorbed by lime stone slurry, blasted in the reaction tank of absorption tower bottom
Air force oxidation, ultimately generate gypsum crystal, on absorption tower top, flue gas after desulfurization is by demister except deentrainment
After drop, absorption tower is left from top, finally enters chimney.The shortcomings that obvious be present in the above method：System is more and complicated, and it is wrapped
Containing flue gas system, absorption tower system, absorbent preparation system, technique water system, gypsum dehydration system, slurries emptying and recovery system
System, compressed air system and electric-control system；Absorbent induction system, slurry preparation system complexity are huge, and initial investment is costly；
Energy consumption and operating cost are high, and processing cost is about 1500~2000 yuan/ton of SO2；Floor space is big；Erosion corrosion phenomenon is more tight
Weight；Waste water, waste residue are more intractable.As sodium alkali there is also it is same the problem of, waste water caused by sodium-hydroxide method contains Na2SO3、
Na2SO4, NaOH etc. is difficult to handle.For another example organic amine absorption process, it is to use another flue gas desulfurization at present, the technique with
Organic amine is absorbent, by the way of low temperature absorption, desorption under high temperature, by the SO in flue gas2Be sent into after enrichment follow-up sulphur or
Sulfuric acid prepares workshop section, realizes the recycling of the qualified discharge and Sulphur ressource of purifying smoke, and desorbing workshop section at it need to consume largely
Steam (7~10t/t SO2), cost is high, in addition, organic amine liquid is expensive, disposed after failure it is more difficult (containing organic nitrogen,
Burning is easily caused secondary pollution problem).The above method to varying degrees there is desulfuration efficiency is not high, operating cost is expensive,
Floor space is big, desulfurizing byproduct recycles the problems such as difficult, and commercial Application is very restricted.
To solve the above problems, a kind of final products disclosed in Chinese patent literature CN102633237A are the desulfurization of sulfuric acid
The reproducible sulfur method of agent, include pretreatment, the SO of flue gas to be desulfurization2Absorption, desulfurizing agent desorption and to SO2Return
The step such as receipts and extracting sulfuric acid, it uses endogenous steam, the energy of desorption of heat technologic gas replacement desorber of the oxygen content more than 10%
Amount is mainly by entering in the absorbing liquid offer of desorber and the gaseous mixture by desorber discharge, SO2Concentration of volume percent control
System is >=3%.Desulfurizing agent is renewable in such scheme, and it is difficult to solve the problems, such as that desulfurizing byproduct recycles, reduces cost.But
It is in such scheme, is that the heat technologic gas of oxygen content 10% are substituted into the rich solution after vapours absorbs sulfur dioxide,
Although being free of steam in heat technologic gas, the heat will not be worked as to introducing moisture in the gaseous mixture containing sulfur dioxide after desorption
When process gas is by the rich solution, the moisture in rich solution can be taken out of, be mixed into as a vapor in stripping gas, if this is desorbed
Gas is used to prepare liquid SO2, it is also necessary to the liquid SO of high-purity can just be prepared after the stripping gas is dried2, step
It is cumbersome, and be difficult to prepare the higher product liquid SO of purity2, and because the input temp of heat technologic gas is up to 100-400 DEG C,
Substantial amounts of heat is needed its temperature is maintained in the range of 100-400 DEG C, high energy consumption, and also the temperature of heat technologic gas is too high, and it is right
It is high in the requirement of equipment, cause equipment investment high, improve cost.
The content of the invention
Therefore, the technical problem to be solved in the present invention is reclaiming the work of sulfur dioxide in flue gas of the prior art is overcome
The defects of skill desulfuration efficiency is low, product purity is low, high energy consumption and cost are high, so as to provide, a kind of desulfuration efficiency is high, product is pure
Degree is high, energy consumption is low low with cost from containing SO2Recovering liquid SO in flue gas2Technique.
Therefore, the invention provides one kind from containing SO2Recovering liquid SO in flue gas2Technique, comprise the following steps：
(1) SO will be contained2Flue gas through poor sulfur absorbing agent absorption cleaning, the flue gas emptying after purification, absorb SO2It is described poor
Sulfur absorbing agent becomes sulfur-rich absorbent, then to the SO in the sulfur-rich absorbent by the way of air air lift2Desorbed；
(2) desorption SO in recycling step (1)2The sulfur-rich absorbent afterwards is as the poor sulphur in the step (1)
Absorbent is absorbing the SO in flue gas2, desorption caused by be rich in SO2Stripping gas it is compressed, condensation obtain liquid SO2；
Wherein, the absorbent is NHD.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, in the step (1), SO in the flue gas2It is shared
Volume fraction when being 0.05-0.2%, the NHD mass percent is 20-80%.Preferably, the cigarette
The tolerance of gas is 5000kmol/h, SO in the flue gas2When shared volume fraction is 0.1%, the NHD
Mass percent is 20-80%.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, in the step (2), the richness caused by control
Containing SO2Stripping gas in SO2Mass concentration is 2~40%, is then rich in SO by described in2Stripping gas be sent into compressor in carry out
Compress, SO is rich in described in control20.4~the 2MPa of pressure of stripping gas after compression.Preferably, it is described to be rich in SO2Stripping gas in
SO2Mass concentration is 8~30%.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, in the step (2), by the institute after overcompression
State and be rich in SO2Stripping gas be sent into condenser in condensed, control the condenser operation temperature be -10~50 DEG C.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, in the step (2), in addition to will be condensed after
What is obtained contains SO2Gas phase be sent into the step of being separated in membrane separator, the film infiltration is mutually sent back in the compression step
SO is rich in described2Stripping gas mixing be compressed, the film ooze it is remaining mutually send back to be used as in desorption procedure do gas stripping gas use.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, by the membrane separator produce film infiltration mutually and film
Remaining phase is oozed, contains SO into the membrane separator2Gas phase in SO2Mass concentration is 0.1~5%, the membrane separator operation pressure
Power is 0.4~2MPa.
Preferably, the membrane material of the membrane separator is selected from polysulfones or polyether sulfone.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, in the step (1), SO will be contained2Flue gas be sent into
In the absorption tower, through the poor sulfur absorbing agent absorption cleaning in the absorption tower, the temperature of the absorption tower tower reactor is controlled
For 3~80 DEG C, tower top purifying smoke outlet temperature is 3~80 DEG C, and the operating pressure on the absorption tower is preferably 0~100kPa.
Preferably, the operating pressure on the absorption tower is preferably 2~100kPa.Preferably, the operating pressure on the absorption tower is preferably 3
~100kPa.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, in the step (1), by the sulfur-rich absorbent
It is sent into the desorber and is desorbed, the temperature for controlling the desorber tower reactor is 3~80 DEG C, desorbs SO2The richness afterwards
Sulfur absorbing agent temperature is 3~80 DEG C, and the operating pressure of the desorber is -95~100kPa.Preferably, the behaviour of the desorber
It is 0~50kPa to make pressure.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, it is described to contain SO in the step (1)2Flue gas exist
Also include containing SO by described in before purification2Flue gas be sent into chilling tower and washed, cooled and the step of smoke abatement.
It is described from containing SO2Recovering liquid SO in flue gas2Technique, it is described to contain SO2Flue gas after chilling temperature be 3~
80oC, pressure are 0~100kPa.Preferably, it is described to contain SO2Flue gas temperature after chilling is 30~80oC, pressure be 2~
100kPa
Technical solution of the present invention, have the following advantages that：
(1) present invention is from containing SO2Recovering liquid SO in flue gas2Technique, comprise the following steps：(1) SO will be contained2Flue gas
Through poor sulfur absorbing agent absorption cleaning, the flue gas emptying after purification, SO is absorbed2The poor sulfur absorbing agent become sulfur-rich absorbent,
Then to the SO in the sulfur-rich absorbent by the way of air air lift2Desorbed；(2) desorption SO in recycling step (1)2
The sulfur-rich absorbent afterwards is as the poor sulfur absorbing agent in the step (1) absorbing the SO in flue gas2, desorption production
Raw is rich in SO2Stripping gas it is compressed, condensation obtain liquid SO2；Wherein, the absorbent is NHD；Pass through
Above-mentioned technique, using NHD as absorbent, the NHD is not only renewable, saves the energy,
Overcome desulfurizing byproduct processing be difficult to recycle the problem of, and NHD in desorption and regeneration without using height
Warm steam or high-temperature technology gas desorbs, and energy consumption is low, while can also avoid introducing moisture into stripping gas, omit to stripping gas
The step of being dried, you can prepare the liquid SO of high-purity2, also reduced due to high-temperature steam or high-temperature technology gas is not used
Requirement to equipment, equipment investment is low, and cost reduces, and passes through SO in the flue gas after the purification of above-mentioned technique2≤35mg/Nm3,
Acid mist≤20mg/Nm3, reached discharge standard, and the liquid SO prepared2Product purity can reach>95%.
(2) it is of the present invention from containing SO2Recovering liquid SO in flue gas2Technique, in the step (1), the flue gas
Middle SO2When shared volume fraction is 0.05-0.2%, the NHD mass percent is 20-80%, is passed through
The SO in flue gas2When shared volume fraction is 0.05-0.2%, the NHD mass percent is controlled so that
The NHD can absorb the SO in flue gas to greatest extent2, remove the SO in flue gas2, significantly improve flue gas and take off
Sulphur efficiency.
(3) it is of the present invention from containing SO2Recovering liquid SO in flue gas2Technique, in the step (2), control produce
Described be rich in SO2Stripping gas in SO2Mass concentration is 2~40%, is then rich in SO by described in2Stripping gas be sent into compression
It is compressed in machine, SO is rich in described in control20.4~the 2MPa of pressure of stripping gas after compression, passes through the SO in stripping gas2Matter
When amount concentration is 2~40%, SO is rich in described in control2The pressure of stripping gas after compression, it is easy to prepare the liquid of higher purity
SO2。
(4) it is of the present invention from containing SO2Recovering liquid SO in flue gas2Technique, will be through overvoltage in the step (2)
Described after contracting is rich in SO2Stripping gas be sent into condenser in condensed, control the condenser operation temperature be -10~50
DEG C, by controlling condensation temperature so that the liquid SO of preparation2Purity is higher.
(5) it is of the present invention from containing SO2Recovering liquid SO in flue gas2Technique, in the step (2), in addition to will
What is obtained after condensed contains SO2Gas phase be sent into the step of being separated in membrane separator, the pressure is mutually sent in the film infiltration back to
In contracting step SO is rich in described2Stripping gas mixing be compressed, the film ooze it is remaining mutually send back to be used as in desorption procedure do gas
Put forward gas use；By using membrane separator, what is preferably obtained after separation condensation contains SO2Gas phase, by SO therein2Gas phase with
Other constituent of air separate, and collect SO therein2Gas be film infiltration mutually be sent into compressor in be compressed, avoid through cold
What is obtained after solidifying contains SO2Gas phase be discharged into air and pollute air, while SO will be free of2Gas phase be that film oozes and remaining is mutually sent into desorption
Gas stripping gas is used as in tower, the energy is saved, reduces cost.
(6) it is of the present invention from containing SO2Recovering liquid SO in flue gas2Technique, contain SO into the membrane separator2
Gas phase in SO2Mass concentration is 0.1~5%, and the membrane separator operating pressure is 0.4~2MPa, by controlling UF membrane
The operating pressure of device so that contain SO into membrane separator2Gas phase can preferably separate.
(7) it is of the present invention from containing SO2Recovering liquid SO in flue gas2Technique, by selecting polysulfones or polyether sulfone to be made
Membrane material for the SO that is obtained after condensation2Gas phase separating effect it is more excellent.
Brief description of the drawings
, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical scheme of the prior art
The required accompanying drawing used is briefly described in embodiment or description of the prior art, it should be apparent that, in describing below
Accompanying drawing is some embodiments of the present invention, for those of ordinary skill in the art, before creative work is not paid
Put, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is from containing SO described in 3-10 of the embodiment of the present invention2Recovering liquid SO in flue gas2Process chart.
Embodiment
Embodiment 1
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, wherein used contain SO2Cigarette
Gas, the tolerance of the flue gas is 10000kmol/h after measured, and temperature is 130 DEG C, and pressure is 30kPa (G), wherein each group partial volume
Percentage is respectively：N269%, O26.5%, CO215%, SO20.05%, H2O 9.45%, the technique include following step
Suddenly：
(1) SO will be contained2Flue gas be sent into the absorption tower, absorbed through the poor sulfur absorbing agent in the absorption tower net
Change, the absorbent is the NHD that mass percent is 15%, and the temperature for controlling the absorption tower tower reactor is 95
DEG C, tower top purifying smoke outlet temperature is 90 DEG C, and the operating pressure on the absorption tower is 105kPa (G), the flue gas warp after purification
The tower top purifying smoke outlet drain absorbs SO into air2The poor sulfur absorbing agent become sulfur-rich absorbent, will described in
Sulfur-rich absorbent is sent into the desorber, and air is passed through from the desorber bottom of towe to the desorber, described in air passes through
Sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed, the operation pressure of the desorber is controlled in desorption process
Power is 103kPa (G), and the temperature of the desorber tower reactor is 90 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is
89℃；
(2) SO is desorbed in the desorber2The sulfur-rich absorbent regeneration afterwards is into the poor sulfur absorbing agent, reclaiming
The poor sulfur absorbing agent be sent into the absorption tower SO absorbed in flue gas2, and it is rich in SO caused by desorbing2Stripping gas in
SO2Mass concentration is 1%, be sent into compressor in be compressed, after compression be rich in SO2Stripping gas pressure 2.2MPa
(G), it is then fed into condenser and condenses, the condenser operation temperature is -13 DEG C, recovering liquid SO2, obtain final products liquid
State SO2, product purity>95%.
Flue gas after the purification of above-mentioned technique is after measured：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；SO2Recovery
Rate is 88%.
Embodiment 2
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, wherein used contain SO2Flue gas
Data, the tolerance of the flue gas is 1000kmol/h after measured, and temperature is 110 DEG C, and pressure is 15kPa (G), wherein each group partial volume
Percentage is respectively：N273%, O27.3%, CO210%, SO20.2%, H2O 9.5%, the technique include following step
Suddenly：
(1) SO will be contained2Flue gas be sent into the absorption tower, absorbed through the poor sulfur absorbing agent in the absorption tower net
Change, the absorbent is the NHD that mass percent is 90%, and the temperature for controlling the absorption tower tower reactor is 2
DEG C, tower top purifying smoke outlet temperature is 2 DEG C, and the operating pressure on the absorption tower is -0.5kPa (G), the flue gas warp after purification
The tower top purifying smoke outlet drain absorbs SO into air2The poor sulfur absorbing agent become sulfur-rich absorbent, will described in
Sulfur-rich absorbent is sent into the desorber, and air is passed through from the desorber bottom of towe to the desorber, described in air passes through
Sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed, the operation pressure of the regenerator is controlled in desorption process
Power is preferably -98kPa (G), and the temperature of the desorber tower reactor is 2 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards
For 1 DEG C；
(2) SO is desorbed in the desorber2The sulfur-rich absorbent regeneration afterwards is into the poor sulfur absorbing agent, reclaiming
The poor sulfur absorbing agent be sent into the absorption tower SO absorbed in flue gas2, and it is rich in SO caused by desorbing2Stripping gas in
SO2Mass concentration is 41%, be sent into compressor in be compressed, after compression be rich in SO2Stripping gas pressure 0.3MPa
(G), it is then fed into condenser and condenses, the condenser operation temperature is -13 DEG C, recovering liquid SO2, obtain final products liquid
State SO2, product purity>96%.
Flue gas after the purification of above-mentioned technique is after measured：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；SO2Recovery
Rate is 90%.
Embodiment 3
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, as shown in figure 1, in the present embodiment
What is used contains SO2Flue gas data, the tolerance of the flue gas is 5000kmol/h after measured, and temperature is 120 DEG C, pressure 20kPa
(G), wherein each component percent by volume is respectively：N271%, O27.2%, CO213%, SO20.1%, H2O 8.7%, institute
Technique is stated to comprise the following steps：
(1) SO will be contained2Flue gas is sent into the chilling tower, and the chilling tower uses packed tower, through washing, cooling, smoke abatement
The flue gas that the temperature obtained afterwards is 50 DEG C, pressure is 55kPa (G) is sent into the absorption tower, is absorbed through poor sulfur absorbing agent in flue gas
SO2, the absorbent is the NHD that mass percent is 50%, wherein the temperature of the absorbing tower kettle is 40
DEG C, tower top clean gas outlet temperature is 38 DEG C, and the operating pressure on the absorption tower is 3kPa (G), and the absorption tower is plate column,
Purified gas goes out from the absorption tower top row, the sulfur-rich absorbent of gained is sent into the desorber, by the way of air air lift
By the SO in sulfur-rich absorbent2Desorb, being passed through the membrane separator to the desorber from the desorber bottom of towe produces
Film ooze remaining phase, the film ooze it is remaining mutually pass through the sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed, its
Described in desorber tower reactor temperature be 42 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is 36 DEG C, the desorption
The operating pressure 0kPa (G) of tower, the desorber are packed tower；
(2) the poor sulfur absorbing agent obtained after desorbing is returned in the absorption tower, returns to the poor sulphur on the absorption tower
Absorbent temperature is 36 DEG C, by the SO of gained2The stripping gas that mass concentration is 24%, which is sent into compressor, to be compressed, will after compression
Pressure be rich in SO for the described of 1.5MPa (G)2Stripping gas be sent into condenser in condensed, condensation temperature be 45 DEG C, it is cold
High-purity liquid SO is reclaimed after solidifying2(product purity>99.9%) mass concentration obtained after, condensed is 3% SO2Gas phase
Membrane separator is sent into, the membrane separator operating pressure is 1MPa, and the membrane material of the membrane separator is selected from polyether sulfone, caused
Film infiltration mutually returns to suction port of compressor and is rich in SO with described2Stripping gas collect, caused film, which oozes, remaining is mutually sent into the desorber
In do gas stripping gas use.
By above-mentioned technique purification after flue gas after measured, purifying smoke：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；
SO2The rate of recovery be 99%.
Embodiment 4
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, as shown in figure 1, in the present embodiment
What is used contains SO2Flue gas data, the tolerance of the flue gas is 5000kmol/h after measured, and temperature is 110 DEG C, pressure 15kPa
(G), wherein each component percent by volume is respectively：N273%, O27.4%, CO210%, SO20.1%, H2O 9.5%, institute
Technique is stated to comprise the following steps：
(1) SO will be contained2Flue gas is sent into the chilling tower, and the chilling tower uses packed tower, through washing, cooling, smoke abatement
The flue gas that the temperature obtained afterwards is 45 DEG C, pressure is 60kPa (G) is sent into the absorption tower, is absorbed through poor sulfur absorbing agent in flue gas
SO2, the absorbent is the NHD that mass percent is 60%, wherein the temperature of the absorbing tower kettle is 43
DEG C, tower top clean gas outlet temperature is 40 DEG C, and the operating pressure on the absorption tower is 30kPa (G), and the absorption tower is filler
Tower, purified gas go out from the absorption tower top row, the sulfur-rich absorbent of gained are sent into the desorber, using the side of air air lift
Formula is by the SO in sulfur-rich absorbent2Desorb, the membrane separator point is passed through from the desorber bottom of towe to the desorber
Remaining phase is oozed from caused film, film oozes remaining phase and passes through the sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed,
The temperature of wherein described desorber tower reactor is 44 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is 40 DEG C, the solution
The operating pressure 20kPa (G) of tower is inhaled, the desorber is packed tower；
(2) the poor sulfur absorbing agent obtained after desorbing is returned in the absorption tower, returns to the poor sulphur on the absorption tower
Absorbent temperature is 40 DEG C, by the SO of gained2The stripping gas that mass concentration is 18%, which is sent into compressor, to be compressed, after compression
Described be rich in SO2Desorption atmospheric pressure be 1.7MPa (G), be then fed into condenser and condensed, condensation temperature be 40 DEG C,
High-purity liquid SO is reclaimed after condensation2(product purity>99.9%) mass concentration obtained after, condensed is 1.5% SO2's
Gas phase is sent into membrane separator and separated, and the membrane separator operating pressure is 2MPa (G), the membrane material of the membrane separator
Selected from polyether sulfone, caused film infiltration mutually returns to suction port of compressor and is rich in SO with described2Stripping gas collect, caused film oozes remaining
Mutually it is sent into the desorber and does gas stripping gas use.
By above-mentioned technique purification after flue gas after measured, purifying smoke：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；
SO2The rate of recovery be 98%.
Embodiment 5
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, as shown in figure 1, in the present embodiment
What is used contains SO2Flue gas data, the tolerance of the flue gas is 5000kmol/h after measured, and temperature is 130 DEG C, pressure 30kPa
(G), wherein each component percent by volume is respectively：N269%, O26.4%, CO215%, SO20.1%, H2O 9.5%, institute
Technique is stated to comprise the following steps：
(1) SO will be contained2Flue gas is sent into the chilling tower, and the chilling tower uses packed tower, through washing, cooling, smoke abatement
The flue gas that the temperature obtained afterwards is 40 DEG C, pressure is 30kPa (G) is sent into the absorption tower, is absorbed through poor sulfur absorbing agent in flue gas
SO2, the absorbent is the NHD that mass percent is 60%, wherein the temperature of the absorbing tower kettle is 42
DEG C, tower top clean gas outlet temperature is 40 DEG C, and the operating pressure on the absorption tower is 50kPa (G), and the absorption tower is board-like
Tower, purified gas go out from the absorption tower top row, the sulfur-rich absorbent of gained are sent into the desorber, using the side of air air lift
Formula is by the SO in sulfur-rich absorbent2Desorb, the membrane separator point is passed through from the desorber bottom of towe to the desorber
Remaining phase is oozed from caused film, film oozes remaining phase and passes through the sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed,
The temperature of wherein described desorber tower reactor is 43 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is 38 DEG C, the solution
The operating pressure 50kPa (G) of tower is inhaled, the desorber is packed tower；
(2) the poor sulfur absorbing agent obtained after desorbing is returned in the absorption tower, returns to the poor sulphur on the absorption tower
Absorbent temperature is 38 DEG C, by the SO of gained2The stripping gas that mass concentration is 12%, which is sent into compressor, to be compressed, after compression
Described be rich in SO2Desorption atmospheric pressure be 1.2MPa (G), be then fed into condenser and condensed, condensation temperature be 20 DEG C,
High-purity liquid SO is reclaimed after condensation2(product purity>99.9%) mass concentration obtained after, condensed is 0.5% SO2's
Gas phase is sent into membrane separator and separated, and the membrane separator operating pressure is 1.5MPa (G), the membrane material of the membrane separator
Material is selected from polyether sulfone, and caused film infiltration mutually returns to suction port of compressor and is rich in SO with described2Stripping gas collect, caused film oozes
Remaining phase is sent into the desorber and does gas stripping gas use.
By above-mentioned technique purification after flue gas after measured, purifying smoke：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；
SO2The rate of recovery be 97%.
Embodiment 6
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, as shown in figure 1, in the present embodiment
What is used contains SO2Flue gas data, the tolerance of the flue gas is 5000kmol/h after measured, and temperature is 140 DEG C, pressure 35kPa
(G), wherein each component percent by volume is respectively：N272.7%, O26.6%, CO211%, SO20.1%, H2O 9.6%,
The technique comprises the following steps：
(1) SO will be contained2Flue gas is sent into the chilling tower, and the chilling tower uses packed tower, through washing, cooling, smoke abatement
The flue gas that the temperature obtained afterwards is 70 DEG C, pressure is 50kPa (G) is sent into the absorption tower, is absorbed through poor sulfur absorbing agent in flue gas
SO2, the absorbent is the NHD that mass percent is 40%, wherein the temperature of the absorbing tower kettle is 65
DEG C, tower top clean gas outlet temperature is 64 DEG C, and the operating pressure on the absorption tower is 45kPa (G), and the absorption tower is filler
Tower, purified gas go out from the absorption tower top row, the sulfur-rich absorbent of gained are sent into the desorber, using the side of air air lift
Formula is by the SO in sulfur-rich absorbent2Desorb, the membrane separator point is passed through from the desorber bottom of towe to the desorber
Remaining phase is oozed from caused film, film oozes remaining phase and passes through the sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed,
The temperature of wherein described desorber tower reactor is 66 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is 62 DEG C, the solution
The operating pressure 40kPa (G) of tower is inhaled, the desorber is plate column；
(2) the poor sulfur absorbing agent obtained after desorbing is returned in the absorption tower, returns to the poor sulphur on the absorption tower
Absorbent temperature is 62 DEG C, by the SO of gained2The stripping gas that mass concentration is 8%, which is sent into compressor, to be compressed, after compression
Described be rich in SO2Desorption atmospheric pressure be 1.8MPa (G), be then fed into condenser and condensed, condensation temperature be 30 DEG C,
High-purity liquid SO is reclaimed after condensation2(product purity>99.9%) mass concentration obtained after, condensed is 0.85% SO2's
Gas phase is sent into membrane separator and separated, and the membrane separator operating pressure is 0.8MPa (G), the membrane material of the membrane separator
Material is selected from polysulfones, and caused film infiltration mutually returns to suction port of compressor and is rich in SO with described2Stripping gas collect, caused film oozes remaining
Mutually it is sent into the desorber and does gas stripping gas use.
By above-mentioned technique purification after flue gas after measured, purifying smoke：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；
SO2The rate of recovery be 96%.
Embodiment 7
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, as shown in figure 1, in the present embodiment
What is used contains SO2Flue gas data, the tolerance of the flue gas is 5000kmol/h after measured, and temperature is 140 DEG C, pressure 35kPa
(G), wherein each component percent by volume is respectively：N272.7%, O26.6%, CO211%, SO20.1%, H2O 9.6%,
Comprise the following steps：
(1) SO will be contained2Flue gas is sent into the chilling tower, and the chilling tower uses packed tower, through washing, cooling, smoke abatement
The flue gas that the temperature obtained afterwards is 3 DEG C, pressure is 0kPa (G) is sent into the absorption tower, is absorbed through poor sulfur absorbing agent in flue gas
SO2, the absorbent is the NHD that mass percent is 20%, wherein the temperature of the absorbing tower kettle is 3
DEG C, tower top clean gas outlet temperature is 3 DEG C, and the operating pressure on the absorption tower is 0kPa (G), and the absorption tower is packed tower,
Purified gas goes out from the absorption tower top row, the sulfur-rich absorbent of gained is sent into the desorber, by the way of air air lift
By the SO in sulfur-rich absorbent2Desorb, being passed through the membrane separator to the desorber from the desorber bottom of towe separates
Caused film oozes remaining phase, and film oozes remaining phase and passes through the sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed, its
Described in desorber tower reactor temperature be 3 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is 3 DEG C, the desorber
Operating pressure -95kPa (G), the desorber is plate column；
(2) the poor sulfur absorbing agent obtained after desorbing is returned in the absorption tower, returns to the poor sulphur on the absorption tower
Absorbent temperature is 3 DEG C, by the SO of gained2The stripping gas that mass concentration is 2%, which is sent into compressor, to be compressed, after compression
It is described to be rich in SO2Desorption atmospheric pressure be 0.4MPa (G), be then fed into condenser and condensed, condensation temperature be -10 DEG C,
High-purity liquid SO is reclaimed after condensation2(product purity>98.5%) mass concentration obtained after, condensed is 0.1% SO2's
Gas phase is sent into membrane separator and separated, and the membrane separator operating pressure is 0.4MPa (G), the membrane material of the membrane separator
Material is selected from polysulfones, and caused film infiltration mutually returns to suction port of compressor and is rich in SO with described2Stripping gas collect, caused film oozes remaining
Mutually it is sent into the desorber and does gas stripping gas use.
By above-mentioned technique purification after flue gas after measured, purifying smoke：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；
SO2The rate of recovery be 94%.
Embodiment 8
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, as shown in figure 1, in the present embodiment
What is used contains SO2Flue gas data, the tolerance of the flue gas is 5000kmol/h after measured, and temperature is 120 DEG C, pressure 20kPa
(G), wherein each component percent by volume is respectively：N271%, O27.2%, CO213%, SO20.1%, H2O 8.7%, bag
Include following steps：
(1) SO will be contained2Flue gas is sent into the chilling tower, and the chilling tower uses packed tower, through washing, cooling, smoke abatement
The flue gas that the temperature obtained afterwards is 80 DEG C, pressure is 100kPa (G) is sent into the absorption tower, is absorbed through poor sulfur absorbing agent in flue gas
SO2, the absorbent is the NHD that mass percent is 80%, wherein the temperature of the absorbing tower kettle is 80
DEG C, tower top clean gas outlet temperature is 80 DEG C, and the operating pressure on the absorption tower is 100kPa (G), and the absorption tower is filler
Tower, purified gas go out from the absorption tower top row, the sulfur-rich absorbent of gained are sent into the desorber, using the side of air air lift
Formula is by the SO in sulfur-rich absorbent2Desorb, the membrane separator point is passed through from the desorber bottom of towe to the desorber
Remaining phase is oozed from caused film, film oozes remaining phase and passes through the sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed,
The temperature of wherein described desorber tower reactor is 80 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is 80 DEG C, the solution
The operating pressure 100kPa (G) of tower is inhaled, the desorber is plate column；
(2) the poor sulfur absorbing agent obtained after desorbing is returned in the absorption tower, returns to the poor sulphur on the absorption tower
Absorbent temperature is 80 DEG C, by the SO of gained2The stripping gas that mass concentration is 40%, which is sent into compressor, to be compressed, after compression
Described be rich in SO2Desorption atmospheric pressure be 2MPa (G), be then fed into condenser and condensed, condensation temperature be 50 DEG C, it is cold
High-purity liquid SO is reclaimed after solidifying2(product purity>98.9%) mass concentration obtained after, condensed is 5% SO2Gas phase
It is sent into membrane separator and is separated, the membrane separator operating pressure is 2MPa (G), and the membrane material of the membrane separator is selected from
Polysulfones, caused film infiltration mutually return to suction port of compressor and are rich in SO with described2Stripping gas collect, caused film, which oozes, remaining to be mutually sent into
Gas stripping gas use is done in the desorber.
By above-mentioned technique purification after flue gas after measured, purifying smoke：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；
SO2The rate of recovery be 95%.
Embodiment 9
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, as shown in figure 1, in the present embodiment
What is used contains SO2Flue gas data, the tolerance of the flue gas is 5000kmol/h after measured, and temperature is 140 DEG C, pressure 35kPa
(G), wherein each component percent by volume is respectively：N272.7%, O26.6%, CO211%, SO20.1%, H2O 9.6%,
Comprise the following steps：
(1) SO will be contained2Flue gas is sent into the chilling tower, and the chilling tower uses packed tower, through washing, cooling, smoke abatement
The flue gas that the temperature obtained afterwards is 60 DEG C, pressure is 2kPa (G) is sent into the absorption tower, is absorbed through poor sulfur absorbing agent in flue gas
SO2, the absorbent is the NHD that mass percent is 60%, wherein the temperature of the absorbing tower kettle is 60
DEG C, tower top clean gas outlet temperature is 58 DEG C, and the operating pressure on the absorption tower is 2kPa (G), and the absorption tower is packed tower,
Purified gas goes out from the absorption tower top row, the sulfur-rich absorbent of gained is sent into the desorber, by the way of air air lift
By the SO in sulfur-rich absorbent2Desorb, being passed through the membrane separator to the desorber from the desorber bottom of towe separates
Caused film oozes remaining phase, and film oozes remaining phase and passes through the sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed, its
Described in desorber tower reactor temperature be 65 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is 63 DEG C, the desorption
The operating pressure 0kPa (G) of tower, the desorber are plate column；
(2) the poor sulfur absorbing agent obtained after desorbing is returned in the absorption tower, returns to the poor sulphur on the absorption tower
Absorbent temperature is 63 DEG C, by the SO of gained2The stripping gas that mass concentration is 30%, which is sent into compressor, to be compressed, after compression
Described be rich in SO2Desorption atmospheric pressure be 1MPa (G), be then fed into condenser and condensed, condensation temperature be 10 DEG C, it is cold
High-purity liquid SO is reclaimed after solidifying2(product purity>99.9%) mass concentration obtained after, condensed is 2% SO2Gas phase
It is sent into membrane separator and is separated, the membrane separator operating pressure is 1MPa (G), and the membrane material of the membrane separator is selected from
Polyether sulfone, caused film infiltration mutually return to suction port of compressor and are rich in SO with described2Stripping gas collect, caused film, which oozes, remaining mutually to be sent
Enter and gas stripping gas use is done in the desorber.
By above-mentioned technique purification after flue gas after measured, purifying smoke：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；
SO2The rate of recovery be 98%.
Embodiment 10
One kind is present embodiments provided from containing SO2Recovering liquid SO in flue gas2Technique, flow is as shown in figure 1, this implementation
What is used in example contains SO2Flue gas data, the tolerance of the flue gas is 5000kmol/h after measured, and temperature is 140 DEG C, and pressure is
35kPa (G), wherein each component percent by volume are respectively：N272.7%, O26.6%, CO211%, SO20.1%, H2O
9.6%, comprise the following steps：
(1) SO will be contained2Flue gas is sent into the chilling tower, and the chilling tower uses packed tower, through washing, cooling, smoke abatement
The flue gas that the temperature obtained afterwards is 40 DEG C, pressure is 55kPa (G) is sent into the absorption tower, is absorbed through poor sulfur absorbing agent in flue gas
SO2, the absorbent is the NHD that mass percent is 60%, wherein the temperature of the absorbing tower kettle is 38
DEG C, tower top clean gas outlet temperature is 35 DEG C, and the operating pressure on the absorption tower is 50kPa (G), and the absorption tower is filler
Tower, purified gas go out from the absorption tower top row, the sulfur-rich absorbent of gained are sent into the desorber, using the side of air air lift
Formula is by the SO in sulfur-rich absorbent2Desorb, the membrane separator point is passed through from the desorber bottom of towe to the desorber
Remaining phase is oozed from caused film, film oozes remaining phase and passes through the sulfur-rich absorbent, to the SO in the sulfur-rich absorbent2Desorbed,
The temperature of wherein described desorber tower reactor is 35 DEG C, control desorption SO2The sulfur-rich absorbent temperature afterwards is 33 DEG C, the solution
The operating pressure 50kPa (G) of tower is inhaled, the desorber is plate column；
(2) the poor sulfur absorbing agent obtained after desorbing is returned in the absorption tower, returns to the poor sulphur on the absorption tower
Absorbent temperature is 33 DEG C, by the SO of gained2The stripping gas that mass concentration is 20%, which is sent into compressor, to be compressed, after compression
Described be rich in SO2Desorption atmospheric pressure be 1.5MPa (G), be then fed into condenser and condensed, condensation temperature be 30 DEG C,
High-purity liquid SO is reclaimed after condensation2(product purity>99.9%) mass concentration obtained after, condensed is 4% SO2Gas
Mutually it is sent into membrane separator and is separated, the membrane separator operating pressure is 1.6MPa (G), the membrane material of the membrane separator
Selected from polyether sulfone, caused film infiltration mutually returns to suction port of compressor and is rich in SO with described2Stripping gas collect, caused film oozes remaining
Mutually it is sent into the desorber and does gas stripping gas use.
By above-mentioned technique purification after flue gas after measured, purifying smoke：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；
SO2The rate of recovery be 99.6%.
Comparative example 1
The present embodiment is similar to Example 10, differs only in poor sulfur absorbing agent difference, its poor sulphur used in it and absorbs
Agent is 30% by monoethanolamine mass percent, and NHD mass percent is 45% and water quality percentage is 35%
Composition.Flue gas after purification is after measured：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；SO2The rate of recovery be 70%, recovery is high
Purity liquid SO2Product purity>80%.
Comparative example 2
The present embodiment is similar to Example 10, differs only in poor sulfur absorbing agent difference, its poor sulphur used in it and absorbs
Agent is the solution D in the test 5 disclosed in CN105848757A in absorbent specification, i.e., is by acid amides-Hep mass percents
13%, 1 equivalent that NHD mass percent is 20% and thermal-stable salt (Dohep) HSS/mole, remaining is
Water forms.Flue gas after purification is after measured：SO2≤35mg/Nm3, acid mist≤20mg/Nm3；SO2The rate of recovery be 75%, recovery
High-purity liquid SO2Product purity>85.6%.
Obviously, above-described embodiment is only intended to clearly illustrate example, and is not the restriction to embodiment.It is right
For those of ordinary skill in the art, can also make on the basis of the above description it is other it is various forms of change or
Change.There is no necessity and possibility to exhaust all the enbodiments.And the obvious change thus extended out or
Among changing still in the protection domain of the invention.
Claims (10)
1. one kind is from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that comprise the following steps：
(1) SO will be contained2Flue gas through poor sulfur absorbing agent absorption cleaning, the flue gas emptying after purification, absorb SO2The poor sulphur inhale
Receive agent and become sulfur-rich absorbent, then to the SO in the sulfur-rich absorbent by the way of air air lift2Desorbed；
(2) desorption SO in recycling step (1)2The sulfur-rich absorbent afterwards is as the poor sulfur absorbing agent in the step (1)
To absorb the SO in flue gas2, desorption caused by be rich in SO2Stripping gas it is compressed, condensation obtain liquid SO2；
Wherein, the absorbent is NHD.
It is 2. according to claim 1 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that in the step
(1) in, SO in the flue gas2When shared volume fraction is 0.05-0.2%, the NHD mass percent
For 20-80%.
It is 3. according to claim 1 or 2 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that in the step
Suddenly it is described caused by control to be rich in SO in (2)2Stripping gas in SO2Mass concentration is 2~40%, is then rich in SO by described in2
Stripping gas be sent into compressor in be compressed, control described in be rich in SO20.4~the 2MPa of pressure of stripping gas after compression.
4. according to claim any one of 1-3 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that
In the step (2), SO will be rich in described in after overcompression2Stripping gas be sent into condenser in condensed, described in control
Condenser operation temperature is -10~50 DEG C.
5. according to claim any one of 1-4 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that
In the step (2), in addition to will be condensed after obtain contain SO2Gas phase be sent into the step of being separated in membrane separator,
Produce film infiltration mutually by the membrane separator and film ooze remaining phase, the film infiltration mutually send back in the compression step with the richness
Containing SO2Stripping gas mixing be compressed, the film ooze it is remaining mutually send back to be used as in desorption procedure do gas stripping gas use.
It is 6. according to claim 5 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that enter the film
Separator contains SO2Gas phase in SO2Mass concentration is 0.1~5%, and the membrane separator operating pressure is 0.4~2MPa.
7. according to claim any one of 1-6 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that
In the step (1), SO will be contained2Flue gas be sent into the absorption tower, inhaled through the poor sulfur absorbing agent in the absorption tower
Purification is received, the temperature for controlling the absorption tower tower reactor is 3~80 DEG C, and tower top purifying smoke outlet temperature is 3~80 DEG C, the suction
The operating pressure for receiving tower is 0~100kPa.
8. according to claim any one of 1-7 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that
In the step (1), the sulfur-rich absorbent is sent into the desorber and desorbed, controls the temperature of the desorber tower reactor
Spend for 3~80 DEG C, desorb SO2The sulfur-rich absorbent temperature afterwards is 3~80 DEG C, and the operating pressure of the desorber is -95
~100kPa.
9. according to claim any one of 1-8 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that
It is described to contain SO in the step (1)2Flue gas before purification also include will described in contain SO2Flue gas be sent into chilling tower in carry out
The step of washing, cooling and smoke abatement.
It is 10. according to claim 9 from containing SO2Recovering liquid SO in flue gas2Technique, it is characterised in that it is described to contain SO2
Flue gas temperature after chilling is 3~80 DEG C, and pressure is 2~100kPa.
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| CN201611026242.3A CN107335322A (en) | 2016-11-18 | 2016-11-18 | One kind is from containing SO2Recovering liquid SO in flue gas2Technique |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201611026242.3A CN107335322A (en) | 2016-11-18 | 2016-11-18 | One kind is from containing SO2Recovering liquid SO in flue gas2Technique |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108744907A (en) * | 2018-06-27 | 2018-11-06 | 湖北鼎创泰裕科技有限公司 | A kind of exhaust gas treating method and processing unit containing sulfur dioxide |
| CN113694676A (en) * | 2021-07-23 | 2021-11-26 | 河北光兴半导体技术有限公司 | Waste gas treatment equipment and glass production system |
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| CN1228715A (en) * | 1996-09-03 | 1999-09-15 | 孟山都公司 | Selective removal and recovery of sulfur dioxide from effluent gases using organic phosphorous solvents |
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2016
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1228715A (en) * | 1996-09-03 | 1999-09-15 | 孟山都公司 | Selective removal and recovery of sulfur dioxide from effluent gases using organic phosphorous solvents |
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| A.Г.阿美林 著: "《硫酸制造》", 30 April 1959 * |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108744907A (en) * | 2018-06-27 | 2018-11-06 | 湖北鼎创泰裕科技有限公司 | A kind of exhaust gas treating method and processing unit containing sulfur dioxide |
| CN113694676A (en) * | 2021-07-23 | 2021-11-26 | 河北光兴半导体技术有限公司 | Waste gas treatment equipment and glass production system |
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