CN105935540A - Apparatus and method for removing and recovering sulfur dioxide in mixed gas - Google Patents
Apparatus and method for removing and recovering sulfur dioxide in mixed gas Download PDFInfo
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- CN105935540A CN105935540A CN201610383137.9A CN201610383137A CN105935540A CN 105935540 A CN105935540 A CN 105935540A CN 201610383137 A CN201610383137 A CN 201610383137A CN 105935540 A CN105935540 A CN 105935540A
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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
- B01D53/1406—Multiple stage absorption
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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
- B01D53/1418—Recovery of products
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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
- B01D53/1425—Regeneration of liquid absorbents
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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
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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
- B01D53/1493—Selection of liquid materials for use as absorbents
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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
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/30—Ionic liquids and zwitter-ions
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- 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
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Abstract
The invention discloses an apparatus for removing and recovering sulfur dioxide in a mixed gas. The apparatus comprises a hypergravity desulphurization device, a tail gas absorption tower, an absorbent cycle storage tank, a lean solution tank, a heat exchanger, a regeneration tower, a circulating pump, a lean solution pump, a rich solution pump, a lean solution cooler, a regeneration tower cooler and a regeneration tower separator which are connected in a certain manner. The invention also discloses a method for removing and recovering sulfur dioxide in the mixed gas through using the apparatus. The apparatus and the method have the advantages of simple structure, high desulphurization efficiency, low production cost, high safety and environmental protection.
Description
Technical field
The present invention relates to tail gas disposal technique field, be specifically related to a kind of for removing and reclaim sulfur dioxide in mixed gas
Devices and methods therefor.
Background technology
2005, China's sulfur dioxide (SO2) emissions total amount was up to 25,490,000 tons, ranks first in the world, and sulfur dioxide (SO2) emissions cause
Economic loss be about 500,000,000,000 yuan, its economic loss accounts for the 2.6% of GDP.Sulfur dioxide pollution has become restriction
China's economy, the key factor of social sustainable development, control sulfur dioxide pollution imperative.
Flue gas desulfurization (FGD) is the desulfurization method of the most unique large-scale commercial application, is to control titanium dioxide
The technical way of sulphur pollution.The main flue gas desulfurization technique of domestic application mainly has " the limestone-gypsum of external introduction
Wet method ", " rotary spraying and drying method " and the domestic dust removal integrated technology of simple desulfurization.All there is improvement SO in these methods2
While pollution, the side-product of generation gets nowhere without market, can bring residue contamination, ammonia and nitrogen pollution, increase CO2 simultaneously
The environmental issues such as discharge.
Wherein wet desulfurization of flue gas by limestone-gypsum method Technology is the prevailing technology technology of China, according to statistics, put into operation,
In the flue gas desulphurization Technology built, Gypsum Wet technology accounts for more than 90%.This technology exists such as
Lower two shortcomings: the value of (1) by-produced gypsum recycling is little, it has to abandon process, create new taking off
Sulfur Gypsum Fibrosum pollutes.(2) often process one ton of sulfur dioxide and to discharge 0.7 ton of carbon dioxide, administer the titanium dioxide in flue gas
Sulphur pollution, has increased again the discharge of greenhouse gases carbon dioxide newly.
In recent years, along with the development of high-gravity technology, high gravity desulfurization equipment such as cross_flow rotating packed bed, hypergravity machine
It is widely used Deng in flue gas desulfurization.High gravity desulfurization equipment utilizes gas-liquid strengthening mass transfer contact to realize,
It is that the multiple dust removal mechanisms such as centrifugal sedimentation, filtration, machinery rotary collision, inertial collision capture and diffusion, moisture film are combined in
The separation of flow cleaner of one.High gravity desulfurization equipment greatly reduce can desulphurization plant dimension and weight, the most by force
Change mass transfer, diabatic process, improve desulfuration efficiency.
Such as China Patent Publication No. CN 102049176 A, denomination of invention: adopting high-gravity solvent cycle absorption method flue gas desulfurization
Technological process.This invention by cross_flow rotating packed bed at the flue gas desulfurization course of the desulfurization solvent such as ionic liquid, organic amine
And the application in desulfurization solvent regenerative process, and the gas such as nitrogen, air is used to participate in desulfurization solvent as gas stripping gas
The desorbing of SO 2 and the regeneration of desulfurization solvent, and combine the filtration, purification of desulfurization solvent, adsorption cleaning and desalination purification skill
Art, defines adopting high-gravity solvent cycle absorption method flue gas desulfurization technique.Weak point is that technological process is long, and operation is many, behaviour
Make loaded down with trivial details, operating cost is high, and produces a large amount of waste water and mud in running, not environmentally.
Summary of the invention
The present invention is directed to the deficiency that prior art exists, it is provided that a kind of technique is simple, desulfuration efficiency is high, production cost is low,
Safety and environmental protection for removing and reclaim the devices and methods therefor of sulfur dioxide in mixed gas.
For achieving the above object, the technical solution used in the present invention is: one is used for removing and reclaim dioxy in mixed gas
Change the device of sulfur, inhale tower, absorbent circulating storage groove, lean flow container, heat exchanger, again including high gravity desulfurization device, tail
Raw tower, circulating pump, lean pump, rich solution pump, lean solution cooler, regenerator cooler and regenerator separator, described
The gas phase import that the gaseous phase outlet of high gravity desulfurization device inhales tower with described tail is connected, and described high gravity desulfurization device leads to
Crossing described rich solution pump to be connected with the rich solution import of described heat exchanger, the rich solution of described heat exchanger exports with described
The rich solution import of regenerator be connected, the top gaseous phase of described regenerator exports by described regenerator cooler and institute
The import of the regenerator separator stated connects, the liquid-phase outlet of described regenerator separator and the coolant of described regenerator
Import connects, and the tower bottoms outlet of described regenerator is connected with the lean solution import of described heat exchanger, described heat friendship
The lean solution outlet of parallel operation is sequentially connected with described lean flow container and described lean pump by described lean solution cooler, described
Lean solution delivery side of pump respectively with the absorbent entrance of described absorbent circulating storage groove, described tail inhale tower absorbent enter
Mouth connects, and described tail is inhaled the tower bottoms outlet of tower and is connected with the rich solution import of described absorbent circulating storage groove, described
The outlet of absorbent circulating storage groove is connected with described high gravity desulfurization device absorbent entrance by described circulating pump.
Described high gravity desulfurization device is preferably hypergravity machine.
The present invention also provides for using said apparatus removing and reclaiming the method for sulfur dioxide in mixed gas, including walking as follows
Rapid:
A () sulfur-bearing gaseous mixture enters high gravity desulfurization device, be fully contacted with absorbent, the SO in gas2With absorption
Agent reaction is absorbed, and obtains desulfurization and absorbs rich solution and the tail gas after partial desulfurization, desulfurization absorb rich solution through rich solution pump,
Heat exchanger, to regenerator, adds Thermal desorption at regenerator through stripped vapor, obtains regenerative mixed gas and regenerator tower reactor
Liquid, regenerative mixed gas obtains SO through regenerator cooler, regenerator separator cooled dehydrated2Product；
The b tail gas after partial desulfurization that () step (a) obtains enters tail and inhales tower, enters with from tower top in tail inhales tower
The absorbent counter current contacting entered, absorbs the SO in tail gas further2, obtain desulfurization and absorb lean solution and purify gas, will purify
Gas inhales tower top qualified discharge from tail.
Described sulfur-bearing mixture temperature is preferably 40～60 DEG C.
Described absorbent can be selected for the one in guanidine, imidazoles, pyridines and alcamines plasma liquid-absorbant or
Several, preferably 1,1,3,3-tetramethyl guanidine lactate, ethanolamine and acetate mixture, diethanolamine and lactic mixt
In one.
Described tail is inhaled tower temperature and is preferably controlled to 30～50 DEG C, and the tail gas after partial desulfurization is preferred with the mass ratio of absorbent
For 1:1～3.
Described high gravity desulfurization unit temp is preferably controlled to 30～70 DEG C.
Described regenerator temperature is preferably controlled to 100～130 DEG C, and pressure is preferably controlled to 30～70KPa.
Described lean solution chiller temperature is preferably controlled to 20～40 DEG C, and described regenerator chiller temperature is preferably controlled to
20～40 DEG C.
As the preferred embodiment of the present invention, regenerator tower bottoms tentatively can be lowered the temperature through heat exchanger, then through lean solution
Cooler enters in lean solution tank after lowering the temperature further, then pressurizes through lean pump, returns to tail and inhales tower absorbent entrance, successively
Cyclic absorption.Regenerator tower bottoms is not up to saturated solution state, returns it to tail and inhales tower continuation absorption SO2, permissible
Make absorbent recycle, reduce production cost, and reduce three waste discharge.
As the preferred embodiment of the present invention, desulfurization can be absorbed lean solution and return to surpass through absorbent circulating storage groove, circulating pump
Gravity desulfurizer, successively cyclic absorption.The desulfurization absorption lean solution obtained from tail suction tower is not up to saturated solution state, will
It returns to high gravity desulfurization device and continues to absorb SO2, on the one hand absorbent can be made to recycle, reduce production cost；
On the other hand double absorption can make continuation absorb SO2After solution reach saturated, and then in subsequent regeneration tower reclaim height
The SO of concentration2Time, improve organic efficiency.
The present invention uses high gravity desulfurization device to carry out desulfurization, under Elevated Gravity, and the intermolecular diffusion of different size and phase
Between mass transport process all than conventional articulated gravity more much faster, it is possible to realize good gas-to-liquid contact and microcosmic mixing, reach
SO2Deep removal.
Absorbent in the present invention is to SO2Gas has good absorption and desorption ability, absorbs titanium dioxide at low temperatures
Sulfur, regenerates out by sulfur dioxide in absorbent under high temperature, thus reaches SO in removing and recovered flue gas2Purpose.This
Absorbent in invention can recycle, and reduce further production cost.
The present invention is used for removing and reclaim sulfur dioxide in mixed gas, is possible not only to reach SO2Deep removal, and
The SO of recyclable high concentration2Gas, has good Social and economic benef@.
Compared with prior art, the invention have the advantages that
1, simple in construction, desulfuration efficiency height, when the present invention is used for removing and reclaiming sulfur dioxide in mixed gas, produce
Stable and reliable operation, operating condition is gentle, it is achieved that SO2Deep removal；
2, production cost is low, good in economic efficiency, when the present invention is used for removing and reclaiming sulfur dioxide in mixed gas, no
Only fume treatment cost is relatively low, SO2Removal efficiency is high, and can reclaim purity SO more than 99.5%2, and inhale
Receiving agent can recycle, reduce further production cost, economic and social benefit is notable；
3, the three wastes are few, safety and environmental protection, and the present invention is in efficient removal SO2, reclaim the SO of high concentration2While, without extra
Side-product produce, absorbent can recycle, and three waste discharge is few, environmental friendliness, meets the development of environmental protection
Requirement.
Accompanying drawing explanation
Fig. 1 is the process chart of the present invention.
In figure: high gravity desulfurization device 1, tail inhale tower 2, absorbent circulating storage groove 3, lean flow container 4, heat exchanger 5,
Regenerator 6, circulating pump 7, lean pump 8, rich solution pump 9, lean solution cooler 10, regenerator cooler 11, regenerator
Separator 12
Detailed description of the invention
By the following examples the present invention is explained in further detail, but the invention is not limited in this.Any with this
Based on invention, for realizing essentially identical technique effect, done simple change, equivalent or modification etc.,
All contain within protection scope of the present invention.
As it is shown in figure 1, the present invention for removing and reclaim the device of sulfur dioxide in mixed gas, take off including hypergravity
Sulfur device 1, tail inhale tower 2, absorbent circulating storage groove 3, lean flow container 4, heat exchanger 5, regenerator 6, circulating pump 7,
Lean pump 8, rich solution pump 9, lean solution cooler 10, regenerator cooler 11 and regenerator separator 12, hypergravity takes off
The gas phase import that the gaseous phase outlet of sulfur device 1 inhales tower 2 with tail is connected, and high gravity desulfurization device 1 is by rich solution pump 9 and warm
The rich solution import of exchanger 5 connects, and the rich solution outlet of heat exchanger 5 is connected with the rich solution import of regenerator 6, regenerator
The top gaseous phase outlet of 6 is connected by the import of regenerator cooler 11 with regenerator separator 12, regenerator separator
The liquid-phase outlet of 12 is connected with the cooling liquid inlet of regenerator 6, and the tower bottoms outlet of regenerator 6 is lean with heat exchanger 5
Liquid import is connected, and the lean solution outlet of heat exchanger 5 is connected with lean flow container 4 and lean pump 8 successively by lean solution cooler 10
Connecing, the outlet of lean pump 8 inhales the absorbent entrance of tower 2 even with the absorbent entrance of absorbent circulating storage groove 3, tail respectively
Connecing, tail is inhaled the tower bottoms outlet of tower 2 and is connected with the rich solution import of absorbent circulating storage groove 3, absorbent circulating storage groove 3
Outlet is connected with high gravity desulfurization device 1 absorbent entrance by circulating pump 7.
When using said apparatus removing and reclaim sulfur dioxide in mixed gas, technological process is: driving forward direction lean solution
Tank 4 adds absorbent, squeezes into high gravity desulfurization device 1 respectively by lean pump 8 and tail inhales tower 2, at device
Running is periodically added absorbent.Sulfur-bearing gaseous mixture enters high gravity desulfurization device 1, fully connects with absorbent
Touch, the SO in gas2React with absorbent and absorbed, obtain desulfurization and absorb rich solution and the tail gas after partial desulfurization,
Desulfurization absorption rich solution, through rich solution pump 9, heat exchanger 5 to regenerator 6, adds Thermal desorption at regenerator 6 through stripped vapor,
Obtaining regenerative mixed gas and regenerator tower bottoms, regenerative mixed gas is through regenerator cooler 11, regenerator separator 12
SO is obtained by regenerator separator 12 gaseous phase outlet after cooling, dehydration2Product.Regenerator tower bottoms is through heat exchange
Device 5 is tentatively lowered the temperature, then enters after lean solution cooler 10 is lowered the temperature further in lean solution tank 4, then through lean pump 8
Pressurization, returns to tail and inhales tower 2 absorbent entrance, cyclic absorption successively.Tail gas after partial desulfurization enters tail and inhales tower
2, with the absorbent counter current contacting entered from tower top in tail inhales tower 2, absorb the SO in tail gas further2,
Absorb lean solution to desulfurization and purify gas, purification gas is inhaled tower top qualified discharge from tail.Desulfurization is absorbed lean solution through absorbing
Agent circulating storage groove 3, circulating pump 7 return to high gravity desulfurization device 1, successively cyclic absorption.
Embodiment 1
Sulfur-bearing mixed gas flow is 120000Nm3/ h, temperature is 50 DEG C, SO2Content is 5%.Sulfur-bearing gaseous mixture enters
Enter hypergravity machine 1 (Zhong Chao Machinery Co., Ltd. of Huludao City, Φ 2000*2500), form with diethanolamine and lactic acid
Absorbent be fully contacted, the SO in gas2React with absorbent and absorbed, obtain desulfurization and absorb rich solution and through portion
Dividing the tail gas after desulfurization, hypergravity machine 1 operates temperature and controls to be 70 DEG C, and desulfurization absorbing liquid is handed over through rich solution pump 9, heat
Parallel operation 5 to regenerator 6, adds Thermal desorption at regenerator 6 through stripped vapor, obtains regenerative mixed gas and regenerator tower
Still liquid, regenerator operating condition is: temperature 120 DEG C, pressure 50KPa, regenerative mixed gas is through regenerator cooler
11, regenerator separator 12 cooled dehydrated obtains SO2Product, it is 20 DEG C that regenerator cooler 11 temperature controls.
Regenerator tower bottoms is tentatively lowered the temperature through heat exchanger 5, then enters lean solution tank after lean solution cooler 10 is lowered the temperature further
In 4, then pressurizeing through lean pump 8, return to tail and inhale tower 2 absorbent entrance, cyclic absorption successively, lean solution cools down
It is 30 DEG C that device 10 temperature controls.Tail gas after partial desulfurization enters tail and inhales tower 2, in tail inhales tower 2 and from tower
The absorbent counter current contacting that portion enters, absorbs the SO in tail gas further2, obtain desulfurization and absorb lean solution and purify gas,
Tail is inhaled tower temperature and is controlled to be 30 DEG C, and the tail gas after partial desulfurization is 1:1 with the mass ratio of absorbent.By purification gas from
Tail inhales tower top qualified discharge, inhales top gaseous phase pipe sample analysis from tail, is not detected by SO2.Desulfurization is absorbed lean solution
Hypergravity machine 1, successively cyclic absorption is returned to through absorbent circulating storage groove 3, circulating pump 7.
From regenerator separator 12 gaseous phase outlet sample analysis, SO2Gas purity 99.5%.
Embodiment 2
Sulfur-bearing mixed gas flow is 130000Nm3/ h, temperature is 60 DEG C, SO2Content is 4%.Sulfur-bearing gaseous mixture enters
Enter hypergravity machine 1 (Zhong Chao Machinery Co., Ltd. of Huludao City, Φ 2500*2500), with absorbent 1,1,3,3-tetramethyl
Guanidine lactate is fully contacted, the SO in gas2React with absorbent and absorbed, obtain desulfurization and absorb rich solution and through portion
Dividing the tail gas after desulfurization, hypergravity machine 1 operates temperature and controls to be 55 DEG C, and desulfurization absorbing liquid is handed over through rich solution pump 9, heat
Parallel operation 5 to regenerator 6, adds Thermal desorption at regenerator 6 through stripped vapor, obtains regenerative mixed gas and regenerator tower
Still liquid, regenerator operating condition is: temperature 130 DEG C, pressure 70KPa, regenerative mixed gas is through regenerator cooler
11, regenerator separator 12 cooled dehydrated obtains SO2Product, it is 40 DEG C that regenerator cooler 11 temperature controls.
Regenerator tower bottoms is tentatively lowered the temperature through heat exchanger 5, then enters lean solution tank after lean solution cooler 10 is lowered the temperature further
In 4, then pressurizeing through lean pump 8, return to tail and inhale tower 2 absorbent entrance, cyclic absorption successively, lean solution cools down
It is 20 DEG C that device 10 temperature controls.Tail gas after partial desulfurization enters tail and inhales tower 2, in tail inhales tower 2 and from tower
The absorbent counter current contacting that portion enters, absorbs the SO in tail gas further2, obtain desulfurization and absorb lean solution and purify gas,
Tail is inhaled tower temperature and is controlled to be 35 DEG C, and the tail gas after partial desulfurization is 1:1.5 with the mass ratio of absorbent, will purify gas
Inhale tower top qualified discharge from tail, inhale top gaseous phase pipe sample analysis from tail, be not detected by SO2.Desulfurization is absorbed lean
Liquid returns to hypergravity machine 1, successively cyclic absorption through absorbent circulating storage groove 3, circulating pump 7.
From regenerator separator 12 gaseous phase outlet sample analysis, SO2Gas purity 99.6%.
Embodiment 3
Sulfur-bearing mixed gas flow is 100000Nm3/ h, temperature is 45 DEG C, SO2Content is 8%.Sulfur-bearing gaseous mixture enters
Enter hypergravity machine 1 (Zhong Chao Machinery Co., Ltd. of Huludao City, Φ 2000*2000), form with ethanolamine and acetic acid
Absorbent is fully contacted, the SO in gas2React with absorbent and absorbed, obtain desulfurization and absorb rich solution and through part
Tail gas after desulfurization, hypergravity machine 1 operates temperature and controls to be 40 DEG C, and desulfurization absorbing liquid is through rich solution pump 9, heat exchange
Device 5 to regenerator 6, adds Thermal desorption at regenerator 6 through stripped vapor, obtains regenerative mixed gas and regenerator tower reactor
Liquid, regenerator operating condition is: temperature 110 DEG C, pressure 40KPa, regenerative mixed gas through regenerator cooler 11,
Regenerator separator 12 cooled dehydrated obtains SO2Product, it is 30 DEG C that regenerator cooler 11 temperature controls.Regeneration
Tower tower bottoms is tentatively lowered the temperature through heat exchanger 5, then enters lean solution tank 4 after lean solution cooler 10 is lowered the temperature further
In, then pressurize through lean pump 8, return to tail and inhale tower 2 absorbent entrance, cyclic absorption successively, lean solution cooler
It is 40 DEG C that 10 temperature control.Tail gas after partial desulfurization enters tail and inhales tower 2, in tail inhales tower 2 and from tower top
The absorbent counter current contacting entered, absorbs the SO in tail gas further2, obtain desulfurization and absorb lean solution and purify gas,
Tail is inhaled tower temperature and is controlled to be 40 DEG C, and the mass ratio of the tail gas after partial desulfurization and absorbent is 1:2, by purification gas from
Tail inhales tower top qualified discharge, inhales top gaseous phase pipe sample analysis from tail, is not detected by SO2.Desulfurization is absorbed lean solution
Hypergravity machine 1, successively cyclic absorption is returned to through absorbent circulating storage groove 3, circulating pump 7.
From regenerator separator 12 gaseous phase outlet sample analysis, SO2Gas purity 99.7%.
Embodiment 4
Sulfur-bearing mixed gas flow is 110000Nm3/ h, temperature is 55 DEG C, SO2Content is 7%.Sulfur-bearing gaseous mixture enters
Enter hypergravity machine 1 (Zhong Chao Machinery Co., Ltd. of Huludao City, Φ 2000*2500), with absorbent 1,1,3,3-tetramethyl
Guanidine lactate is fully contacted, the SO in gas2React with absorbent and absorbed, obtain desulfurization and absorb rich solution and through portion
Dividing the tail gas after desulfurization, hypergravity machine 1 operates temperature and controls to be 30 DEG C, and desulfurization absorbing liquid is handed over through rich solution pump 9, heat
Parallel operation 5 to regenerator 6, adds Thermal desorption at regenerator 6 through stripped vapor, obtains regenerative mixed gas and regenerator tower
Still liquid, regenerator operating condition is: temperature 100 DEG C, pressure 30KPa, regenerative mixed gas is through regenerator cooler
11, regenerator separator 12 cooled dehydrated obtains SO2Product, it is 35 DEG C that regenerator cooler 11 temperature controls.
Regenerator tower bottoms is tentatively lowered the temperature through heat exchanger 5, then enters lean solution tank after lean solution cooler 10 is lowered the temperature further
In 4, then pressurizeing through lean pump 8, return to tail and inhale tower 2 absorbent entrance, cyclic absorption successively, lean solution cools down
It is 35 DEG C that device 10 temperature controls.Tail gas after partial desulfurization enters tail and inhales tower 2, in tail inhales tower 2 and from tower
The absorbent counter current contacting that portion enters, absorbs the SO in tail gas further2, obtain desulfurization and absorb lean solution and purify gas,
Tail is inhaled tower temperature and is controlled to be 50 DEG C, and the mass ratio of the tail gas after partial desulfurization and absorbent is 1:3, by purification gas from
Tail inhales tower top qualified discharge, inhales top gaseous phase pipe sample analysis from tail, is not detected by SO2.Desulfurization can be absorbed lean
Liquid returns to hypergravity machine 1, successively cyclic absorption through absorbent circulating storage groove 3, circulating pump 7.
From regenerator separator 12 gaseous phase outlet sample analysis, SO2Gas purity 99.8%.
Claims (10)
1., for removing and reclaim a device for sulfur dioxide in mixed gas, inhale including high gravity desulfurization device, tail
Tower, absorbent circulating storage groove, lean flow container, heat exchanger, regenerator, circulating pump, lean pump, rich solution pump, lean solution are cold
But device, regenerator cooler and regenerator separator, it is characterised in that the gaseous phase outlet of described high gravity desulfurization device with
Described tail is inhaled the gas phase import of tower and is connected, and described high gravity desulfurization device is by described rich solution pump and described heat friendship
The rich solution import of parallel operation connects, and the rich solution outlet of described heat exchanger is connected with the rich solution import of described regenerator, institute
The top gaseous phase outlet of the regenerator stated is connected by the import of described regenerator cooler with described regenerator separator
Connecing, the liquid-phase outlet of described regenerator separator is connected with the cooling liquid inlet of described regenerator, described regenerator
Tower bottoms outlet is connected with the lean solution import of described heat exchanger, and the lean solution of described heat exchanger exports by described
Lean solution cooler is sequentially connected with described lean flow container and described lean pump, and described lean solution delivery side of pump is respectively with described
The absorbent entrance of absorbent circulating storage groove, described tail inhale the absorbent entrance of tower and connect, described tail inhales the tower of tower
The outlet of still liquid is connected with the rich solution import of described absorbent circulating storage groove, and the outlet of described absorbent circulating storage groove is passed through
Described circulating pump is connected with described high gravity desulfurization device absorbent entrance.
The most according to claim 1 for removing and reclaim the device of sulfur dioxide in mixed gas, its feature exists
It is hypergravity machine in described high gravity desulfurization device.
3. using the device removing described in claim 1 and reclaim the method for sulfur dioxide in mixed gas, its feature exists
In comprising the steps:
A () sulfur-bearing gaseous mixture enters high gravity desulfurization device, be fully contacted with absorbent, the SO in gas2Anti-with absorbent
Should be absorbed, obtain desulfurization and absorb rich solution and the tail gas after partial desulfurization, desulfurization absorbs rich solution and hands over through rich solution pump, heat
Parallel operation, to regenerator, adds Thermal desorption at regenerator through stripped vapor, obtains regenerative mixed gas and regenerator tower bottoms, then
Raw gaseous mixture obtains SO through regenerator cooler, regenerator separator cooled dehydrated2Product；
The b tail gas after partial desulfurization that () step (a) obtains enters tail and inhales tower, enters with from tower top in tail inhales tower
Absorbent counter current contacting, absorb further the SO in tail gas2, obtain desulfurization and absorb lean solution and purify gas, gas will be purified
Tower top qualified discharge is inhaled from tail.
The method of sulfur dioxide in removing the most according to claim 3 and recovery mixed gas, it is characterised in that institute
The sulfur-bearing mixture temperature stated is 40～60 DEG C.
The method of sulfur dioxide in removing the most according to claim 3 and recovery mixed gas, it is characterised in that institute
The absorbent stated is 1,1,3,3-tetramethyl guanidine lactate, ethanolamine and acetate mixture, diethanolamine and lactic mixt
In one.
The method of sulfur dioxide in removing the most according to claim 3 and recovery mixed gas, it is characterised in that institute
The tail stated is inhaled tower temperature and is controlled to be 30～50 DEG C, and the tail gas after partial desulfurization is 1:1～3 with the mass ratio of absorbent.
The method of sulfur dioxide in removing the most according to claim 3 and recovery mixed gas, it is characterised in that institute
It is 30～70 DEG C that the high gravity desulfurization unit temp stated controls.
The method of sulfur dioxide in removing the most according to claim 3 and recovery mixed gas, it is characterised in that institute
It is 100～130 DEG C that the regenerator temperature stated controls, and Stress control is 30～70KP, described lean solution chiller temperature control
Being made as 20～40 DEG C, it is 20～40 DEG C that described regenerator chiller temperature controls.
The method of sulfur dioxide in removing the most according to claim 3 and recovery mixed gas, it is characterised in that will
Regenerator tower bottoms is tentatively lowered the temperature through heat exchanger, then enters after lean solution cooler is lowered the temperature further in lean solution tank, then
Pressurize through lean pump, return to tail and inhale tower absorbent entrance, cyclic absorption successively.
The method of sulfur dioxide in removing the most according to claim 3 and recovery mixed gas, it is characterised in that will
Desulfurization absorbs lean solution and returns to high gravity desulfurization device, successively cyclic absorption through absorbent circulating storage groove, circulating pump.
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| CN109621684A (en) * | 2019-01-17 | 2019-04-16 | 北京化工大学 | A kind of device and method that alkylation spent acid recycles |
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