CN102485320A - Device for desulfurizing flue gas by seawater through membrane absorption and its process - Google Patents

Device for desulfurizing flue gas by seawater through membrane absorption and its process Download PDF

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Publication number
CN102485320A
CN102485320A CN2010105729715A CN201010572971A CN102485320A CN 102485320 A CN102485320 A CN 102485320A CN 2010105729715 A CN2010105729715 A CN 2010105729715A CN 201010572971 A CN201010572971 A CN 201010572971A CN 102485320 A CN102485320 A CN 102485320A
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China
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seawater
membrane component
flue gas
absorber
hollow fiber
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CN2010105729715A
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Chinese (zh)
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CN102485320B (en
Inventor
陈颖
关毅鹏
刘国昌
郭春刚
张召才
李晓明
李雪梅
吕经烈
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国家海洋局天津海水淡化与综合利用研究所
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Priority to CN 201010572971 priority Critical patent/CN102485320B/en
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Abstract

The invention discloses a device for desulfurizing flue gas by seawater through membrane absorption and its process, the flue gas is sent to a membrane absorber shell side by a supercharging blower fan, the pretreated seawater enters in a membrane absorber tube side through a sea water pump and is taken as absorption liquid, gas phase and liquid phase form a reaction interface at the micropore of a hollow fiber membrane, SO2 in flue gas is reacted with seawater to generate sulfite and timely is taken away for realizing the flue gas desulphurization. Desulfurized seawater is discharged through aeration sulfur fixation and pH value standard achieving. The device of the invention is composed of a one stage or multistage membrane absorber, the membrane absorber is composed of multi-group curtain type or column type hollow fiber film component group. The process has the characteristics of low air resistance of the device, small power consumption and high desulphurization efficiency. A design of an automatic on-line backwashing and cleaning technology is capable of controlling and mitigating membrane pollution, the device possesses small volume and light weight, and enables modularized integration; the flow velocity of the gas phase and the liquid phase can be independently controlled in a wide scope, and the problem of device corrosion caused by entrainment water vapor in flue gas in a traditional seawater method can be avoided.

Description

Membrane absorption method flue gas desulfurization with seawater device and technology thereof
Technical field
The invention belongs to the crossing domain of air pollution control technique and membrane science technical application, be specifically related to a kind of with seawater as absorption liquid, adopt film absorption technique to remove the system of sulfur dioxide in flue gas.
Background technology
Sulfur dioxide in the atmosphere mainly comes from the burning of fossil fuels such as industrial waste gas, coal and oil.China provides thermal source and electric power resource still to be main flow through fire coal in present and even following quite long period.In recent years, the financial burden that economy development of coastal area causes severe power shortage to bring rapidly increases the weight of, and causes coastal thermoelectricity development swift and violent, has accounted for 1/3rd of thermoelectricity installation total amount at present.The SO of power industry discharging 2Account for 50% of national total release.The famine of China's freshwater resources; Make that the industrialization of Coastal Power Station desalinization, the cooling of seawater direct current and seawater recirculation refrigerating technology is with the obvious advantage; Utilize and promote the flue gas desulfurization with seawater technology; Air contaminant treatment and seawater resources are utilized combination again, both can practice thrift a large amount of fresh water, can reduce SO again 2Discharging is to kill two birds with one stone.
The flue gas desulfurization technique that the coal-burning power plant is ripe can be divided into wet method, dry method and semidry method etc.Wherein dry method and semidry process need consume a large amount of absorbents, and produce solid by-product, and equipment attrition is big, and operation and maintenance cost is high.Ripe wet processing has seawater method and limestone-gypsum method; Compare with limestone-gypsum method, the seawater method can be saved preparation a large amount of fresh water that absorption liquid consumed, but owing to adopt conventional gas absorption equipment (like packed tower, liquid column tower and spray column etc.); Still can't break away from the common problem of wet process of FGD: because gas-liquid two-phase directly contacts in the smoke absorption process; Make this technology be subject to the restriction of hydrodynamics conditions such as liquid flooding, channel and entrainment, cause absorption liquid and smoke distribution inhomogeneous, mass-transfer efficiency is low; And contain a large amount of steam in the discharged flue gas, residual in addition SO 2, therefore have the equipment corrosion problem.Many improvement of tradition flue gas desulfurization technique and equipment, purpose are to make and absorb the tiny increase specific surface of drop, and flue gas flow field is more evenly optimized, and strengthen gas-liquid mass transfer, promote desulfuration efficiency.It is huge that yet the result is an equipment volume, and technology controlling and process is complicated, and investment and operation expense are high.
Publication number is CN101091873A; The Chinese invention patent that its open day is on December 26th, 2007 discloses " a kind of membrane absorption method seawater removes the process of sulfur dioxide in flue gas "; Its technical process is that flue gas is after the dedusting cooling; In the tube side by entering Hollow Fiber Membrane Absorption device after the gas compressor pressure regulation, and keep gas-liquid phase pressure difference in hollow fiber film assembly bubble point pressure scope, its gaseous pressure value is up to 11kPa.Because the vapour lock that Hollow Fiber Membrane Absorption device capillarity is produced is bigger, therefore need flue gas be provided through gas compressor, power consumption is very big.Therefore membrane absorption method removes sour gas research and all is in laboratory stage in the past, is difficult to realize that through engineering approaches uses.
Summary of the invention
To above-mentioned prior art; The present invention provides a kind of membrane absorption method flue gas desulfurization with seawater device, and this device is made up of one or more levels film absorber, and the film absorber is made up of many groups curtain formula or pillar hollow fibre membrane component; Porous hydrophobic property doughnut membrane material provides huge effective gas-liquid contact area; Make this device vapour lock low, power consumption is little, and desulfuration efficiency is high; Device volume is little, and is in light weight, but modularization is integrated; Simultaneously, the invention provides the technology of utilizing said apparatus to carry out flue gas desulfurization, be with seawater as absorption liquid, with gas-liquid membrane component component film absorber, realize flue gas desulfurization.Adopt this technology gas-liquid two-phase evenly to distribute, and can under the situation of gas-liquid two-phase independent operation, make SO in the flue gas 2With the fast reaction of alkalescent seawater, and in time taken away, form the irreversible reaction layer on film surface, gas-liquid mass transfer speed is fast, and desulfuration efficiency is high, and can alleviate or avoid traditional seawater method flue gas to carry a large amount of steam secretly and the equipment corrosion problem that causes.Cooperate PLC control can realize the automatic on-line cleaning, from further control with alleviate film and pollute.
In order to solve the problems of the technologies described above, the technical scheme that membrane absorption method flue gas desulfurization with seawater device of the present invention is achieved is: this device comprises one-level film absorber at least, the sea water preprocessing equipment and sea water pump, the heat exchanger that links to each other successively and ventilation apparatus that link to each other successively; The liquid phase import of said film absorber links to each other with said sea water pump, and the gas phase import of said film absorber links to each other with said ventilation apparatus; The liquid phase outlet of said film absorber links to each other with an aeration tank; Said ventilation apparatus adopts booster fan; Said film absorber adopts a kind of in box gas-liquid contact membranes absorber and the pot type gas-liquid contact membranes absorber, wherein:
Said box gas-liquid contact membranes absorber: comprise hollow fibre membrane component, a casing, be arranged on the baffle plate in the casing and be arranged on the film cleaning part in the casing; Form a film absorber shell side between the wall of said hollow fibre membrane component and casing; Said hollow fibre membrane component is a sheet curtain formula hydrophobic hollow fiber membrane component; Be the network-like described sheet curtain of the multi-disc formula hydrophobic hollow fiber membrane component that is furnished with of grid along vapor phase stream through direction in the said casing; Said sheet curtain formula hydrophobic hollow fiber membrane component is made up of with the membrane component end socket that is sealed in the described sheet curtain of multi-disc formula hydrophobic hollow fiber diaphragm upper/lower terminal the doughnut diaphragm through braiding, and said membrane component end socket is provided with and draws sap cavity; Relatively independent between the every described sheet curtain formula hydrophobic hollow fiber membrane component; Be provided with feed pipe with a plurality of described membrane component end sockets two ends align respectively; Said membrane component end socket two ends are connected to respectively on the feed pipe that aligns with it; The position that aligns at the two ends with each feed pipe on the wall of said casing is provided with an aperture, and casing is stretched out in the two ends of said feed pipe from the aperture that aligns with it; Said baffle plate is the plate of a hollow, and said baffle plate is vertical basically through direction with vapor phase stream, and said baffle plate closely is arranged between the described sheet curtain of multi-disc formula hydrophobic hollow fiber membrane component and the said casing; Said film cleaning part comprises that flatly being arranged on one in the casing cleans feed pipe and a plurality of scavenge pipe, is provided with a plurality of nozzles on the tube wall of said scavenge pipe equably, and a plurality of described scavenge pipes are connected on the described cleaning feed pipe;
Said pot type gas-liquid contact membranes absorber: comprise hollow fibre membrane component, a pot type housing and flatly be arranged on the film cleaning part in the said pot type housing; Form a film absorber shell side between the wall of said hollow fibre membrane component and tank body; Said hollow fibre membrane component is a pillar hydrophobic hollow fiber membrane component; Evenly be furnished with the described pillar hydrophobic hollow fiber membrane component of many groups in the said pot type housing; Be provided with the support bar parallel in every group of pillar hydrophobic hollow fiber membrane component with a central tube; The hole of even distribution some on the tube wall of said central tube; The occupied region area in all holes is greater than or equals the cross-sectional area of said central tube, and the top of said central tube is provided with plug; Hollow-fibre membrane in every group of pillar hydrophobic hollow fiber membrane component is rolled into column through after the yarns, the sealed at both ends casting; Relatively independent between every group of pillar hydrophobic hollow fiber membrane component; The top and bottom of the said pillar hydrophobic hollow fiber membrane component of a part are provided with the bilateral end socket, and the top and bottom of the said pillar hydrophobic hollow fiber of another part membrane component are provided with the threeway end socket; The pipe end of the bilateral end socket on the said pillar hydrophobic hollow fiber membrane component of many groups and the pipe end of threeway end socket interconnect assembling respectively and form path on same horizontal plane; The pillar hydrophobic hollow fiber membrane component that is provided with the threeway end socket all is positioned at the inwall place of said pot type housing; Wherein, the end socket of the top and bottom of the threeway end socket pillar membrane component of the symmetry of two groups on the diagonal all respectively is provided with a free pipe end; Be provided with an aperture in the position that aligns with each free pipe end on the wall of pot type housing, said free pipe end stretches out housing from the aperture that aligns with it; The water conservancy diversion that the top and bottom of the said pillar hydrophobic hollow fiber membrane component of many groups are provided with pillar hydrophobic hollow fiber membrane component supports or supporting construction; Said water conservancy diversion supporting construction includes a plurality of gas phase pod apertures; Said film cleaning part comprises that flatly being arranged on one in the tank body cleans feed pipe and a plurality of scavenge pipe, and the tube wall of said scavenge pipe is provided with a plurality of nozzles, and said a plurality of scavenge pipes are integrated and connected to said feed pipe.
The technical scheme that membrane absorption method flue gas desulfurization with seawater technology of the present invention is achieved is: utilize above-mentioned membrane absorption method flue gas desulfurization with seawater device to carry out flue gas desulfurization, its process is following:
Flue gas is sent into film absorber shell side through booster fan after heat exchanger adopts the cooled with seawater cooling; Get into film absorber tube side as the desulfurization absorption liquid through the pretreated seawater of sea water preprocessing equipment through sea water pump; Gas-liquid two-phase forms reaction interface, SO in the flue gas at the micropore place of hollow-fibre membrane 2Generate sulphite with the seawater reaction; Flue gas after the desulfurization is discharged from the gaseous phase outlet of said film absorber; Meanwhile, the seawater that has sulphite is the solid sulphur of aeration through the aeration tank, and discharge its pH value back up to standard.
Remove the sour gas system with spray column GAS ABSORPTION in the prior art and membrane absorption method in the past and compare, the beneficial effect of membrane absorption method flue gas desulfurization with seawater device of the present invention and technology thereof is:
One of which; The hollow-fibre membrane specific surface that adopts in the flue gas desulfur device of the present invention is huge; The optimized Structure Design of film absorber in addition; Guaranteed uniform gas-liquid distribution, made effective mass transfer area of unit equipment volume reach 10 times~20 times of traditional absorption tower, and the sea water resistance of hydrophobic film material and sour gas etching characteristic are good;
Its two, flue gas desulfurization technique gas-liquid two-phase independent operation of the present invention, the flow velocity control range is wide, no liquid flooding; Flue gas does not directly contact with seawater, and flue gas after desulfurization is not carried a large amount of steam secretly, and the dew-point temperature of discharging flue gas is significantly reduced, and can alleviate or avoid equipment corrosion;
Its three, the film absorber flue gas resistance in the flue gas desulfur device of the present invention is low, the SO of anti-the flue gas 2Concentration and flow attack ability are strong, and the seawater utilization rate is high, and power consumption is little; Film absorber contamination resistance is strong, and desulfuration efficiency is stable, can be according to flue gas SO 2Concentration is regulated desulfurization degree, control SO automatically in 90%~98% scope 2Reach discharge standard.
Description of drawings
Fig. 1 is a membrane absorption method flue gas desulfurization with seawater process chart;
Fig. 2 a is the pillar hydrophobic hollow fiber membrane component sketch map of pot type gas-liquid contact membranes absorber among the present invention;
Fig. 2 b is the pillar hydrophobic hollow fiber membrane component sketch map that has the threeway end socket;
Fig. 2 c is the pillar hydrophobic hollow fiber membrane component sketch map that has the bilateral end socket;
Fig. 2 d is the end socket connected mode sketch map of 9 groups of pillar membrane components in the single-stage pot type film absorber;
Fig. 3 a is the structural representation of the water conservancy diversion gripper shoe of pot type gas-liquid contact membranes absorber among the present invention;
Fig. 3 b is the structural representation of the cleaning part of pot type gas-liquid contact membranes absorber among the present invention;
Fig. 3 c is the structural representation of the base plate of pot type gas-liquid contact membranes absorber among the present invention;
Fig. 4 a is that pot type gas-liquid contact membranes absorber adopts single stage membrane absorber operational mode sketch map among the present invention;
Fig. 4 b adopts single stage membrane absorber back-flushing operation pattern diagram for pot type gas-liquid contact membranes absorber among the present invention;
Fig. 4 c adopts two-stage series connection intergration model sketch map for pot type gas-liquid contact membranes absorber among the present invention;
Fig. 5 a is a box gas-liquid contact membranes absorber perspective view among the present invention;
Fig. 5 b is the sheet curtain formula hydrophobic hollow fiber membrane component sketch map shown in Fig. 5 a;
Fig. 5 c is the sheet curtain formula hydrophobic hollow fiber membrane component sketch map that the constriction shown in Fig. 5 a becomes;
Fig. 6 a is the perspective view of film cleaning part in the box gas-liquid contact membranes absorber among the present invention;
Fig. 6 b is the sketch map of scavenge pipe shown in the box gas-liquid contact membranes of Fig. 6 a absorber;
Fig. 7 is the structure perspective view of box gas-liquid contact membranes absorber middle shell interior panelling among the present invention;
Fig. 8 is the sketch map of box gas-liquid contact membranes absorber operational mode among the present invention;
Fig. 9 is the sketch map of box gas-liquid contact membranes absorber backwash mode among the present invention;
Figure 10 is the sketch map of box gas-liquid contact membranes absorber on-line cleaning pattern among the present invention;
Figure 11 be among the present invention box gas-liquid contact membranes absorber by a two-stage series connection sketch map after integrated.
Among the figure:
1---hollow-fibre membrane 2---yarn
3---central tube 4---cast material
5---support bar 6,7---bilateral end socket
8---pipe tap 9,10---threeway end socket
11---water conservancy diversion gripper shoe 12---draw-in groove hole
13---aperture 14---film cleaning part
15---scavenge pipe 16---nozzle
17---feed pipe 18---base plate
19---cleaning agent outlet 20---pot type housing
21---cleaning agent import 22,23,25,26---import/export of liquid phase entering/outflow pipeline
24---plug
101 to 108---the import/export of liquid phase entering/outflow pipeline
The outlet of 109---cleaning agent import 1110---cleaning agent
111---feed pipe 112---membrane component end socket
113---hollow-fibre membranes 114---clean feed pipe
115---scavenge pipe 116---baffle plate
117---casing 118---feed pipe
122---drawing sap cavity 124---hollow fibre membrane component
I---first order pot type film absorber II---second level pot type film absorber
A---liquid phase B---cleaning agent
C---gas phase
The specific embodiment
Below in conjunction with the accompanying drawing and the specific embodiment the present invention is done to describe in further detail.
As shown in Figure 1, membrane absorption method flue gas desulfurization with seawater device of the present invention, the sea water preprocessing equipment 203 that comprise one-level film absorber 201 at least, links to each other successively and sea water pump 204, the heat exchanger 208 and the ventilation apparatus that link to each other successively; The liquid phase import of said film absorber 201 links to each other with said sea water pump 204, and the gas phase import of said film absorber 201 links to each other with said ventilation apparatus; The liquid phase outlet of said film absorber 201 links to each other with an aeration tank 205; Said ventilation apparatus adopts booster fan 209; Said film absorber 201 adopts a kind of in pot type gas-liquid contact membranes absorbers and the box gas-liquid contact membranes absorber.Wherein, Pot type gas-liquid contact membranes absorber is made up of many groups pillar hydrophobic hollow fiber membrane component; Flow through the successively central tube of the corresponding series connection of film absorber (201-1 to 201-n) of flue gas evenly sprays perpendicular to fiber axis from the circular hole that is distributed on the tube wall; Nuzzle up the hollow-fibre membrane outer wall to external diffusion, and the outer surface along the column curtain type membrane flows to next stage film absorber shell side then, discharges from last one-level.Box gas-liquid contact membranes absorber is made up of many groups sheet curtain formula hydrophobic hollow fiber membrane component; The curtain type membrane sheet forms grid-like network structure along the flue gas direction of flowing through; To guarantee that flue gas is on the vertical cross section of its direction of flowing through; Equably along flowing through the hollow-fibre membrane outer wall perpendicular to the fiber axis direction, the flue gas film absorber (201-1 to 201-n) of flowing through successively; Above-mentioned two types film absorber can confirm that device is made up of several film absorbers according to scale, and it is integrated to be easy to scale design and modularization.The seawater hollow-fibre membrane mesopore of flowing through, flue gas vertical fibers direction of principal axis flows through the hollow-fibre membrane outer wall, and gas-liquid two-phase forms fast reaction interface, SO in the flue gas at the membrane micropore place 2Also in time taken away by Absorption by Sea Water.The aeration processing is carried out, the back up to standard discharging of pH value in the concentrated aeration tank that enters of seawater after the desulfurization.Flue gas after the desulfurization is discharged from the gaseous phase outlet of film absorber.
Film absorber among the present invention adopts the hydrophobic hollow fiber film; Be selected from polytetrafluoroethylene (PTFE), Kynoar, polyvinyl chloride, polysulfones, polyether sulfone, polyether sulphone, polyethylene, polypropylene, polyester, silicon rubber, one or more polyblends or the membrane material that is laminated with.Its perforated membrane maximum diameter of hole scope is 0.001 μ m~2.0 μ m, and wall thickness range is 20 μ m~200 μ m, and porosity ranges is 20%~80%.
Membrane absorption method flue gas desulfurization with seawater technology of the present invention is as shown in Figure 1, as absorption liquid, through pot type or box gas-liquid contact membranes absorber, realizes flue gas desulfurization with seawater.The process of utilizing membrane absorption method flue gas desulfurization with seawater device of the present invention to carry out flue gas desulfurization is: flue gas 207 is sent into film absorber shell side as the desulfurization absorption liquid through booster fan 209 after heat exchanger 208 adopts the cooled with seawater cooling; Get into film absorber tube side through sea water preprocessing equipment 203 pretreated seawater 202 through sea water pump 204; Gas-liquid two-phase forms reaction interface, SO in the flue gas at the micropore place of hollow-fibre membrane 2Generate sulphite with the seawater reaction; Flue gas after the desulfurization is discharged from the gaseous phase outlet of said film absorber 201; Meanwhile, the seawater that has sulphite is the solid sulphur of 205 aerations through the aeration tank, and its pH value back up to standard discharges 206.
In the membrane absorption method flue gas desulfurization with seawater technology of the present invention; The absorption liquid seawater is meant any in the concentrated seawater of seawater, seawater circulation cooling and embrane method desalinization discharging of former seawater, seawater direct current cooling discharging, and its conductivity range is 30000 μ S/cm~80000 μ S/cm; Its pH value is controlled at more than 7.5.Its preliminary treatment is on the natural subsidence basis, to add non-oxidative bactericide processings of killing livestock, and removes the above suspension of 50 μ m through coarse filtration, changes according to raw water quality simultaneously, carries out electrical conductivity, pH value is monitored and adjusting in good time.The desulfurization seawater that the film absorber is discharged with clean seawater and be acid, can sneak into fresh seawater in right amount according to pH value size, carry out aeration simultaneously and handle with fixing SO 2, the seawater behind over recovery (pH>=6.5) enters the sea.Seawater removes SO in the flue gas as absorption liquid 2And the chemical principle of recovery process is following:
When seawater is flowed through the film absorber, absorb the SO in the dissolving flue gas 2, and the generation sulfurous acid hydrogen radical ion that reacts fast, its chemical equation is following:
(1)SO 2(aq)+H 2O→H ++HSO 3 -
Be rich in bicarbonate ion in former seawater or the concentrated seawater and be alkalescent, have stronger buffer capacity, but the hydrogen ion that neutralization reaction (1) produces, and its chemical equation is following:
(2)H ++HCO 3 -→H 2O+CO 2
The sulfurous acid hydrogen radical ion that reaction (1) generates is oxidized to sulfate ion in the aeration tank, the bicarbonate ion neutralization in the fresh seawater that the hydrogen ion that generates is simultaneously sneaked into, thereby with SO 2Be fixed in the seawater and no longer separate out, its chemical equation is following:
(3)HSO 3 -+1/2O 2(aq)+HCO 3 -→SO 4 2-+H 2O+CO 2
When absorption liquid is concentrated seawater, compare, because its salinity, basicity, ionic strength are all higher, to SO with former seawater 2Buffer capacity and absorbability stronger, the chemical reaction enhancer in the absorption process is bigger, so overall mass transfer coefficient is bigger, under the same operation process conditions, the concentrated seawater desulfurization degree is apparently higher than former seawater.
Flue gas in the above-mentioned PROCESS FOR TREATMENT is meant and comprises: the coal-fired flue-gas after dedusting and/or contain SO 2Industrial waste gas, SO wherein 2Concentration range is 50mg/Nm 3~5000mg/Nm 3High-temperature flue gas is reduced to its temperature below 50 ℃ through over-heat-exchanger, gets into the film absorber then and carries out desulfurization, and the flue gas after the desulfurization is through SO 2After concentration and the temperature detection, discharge from the gaseous phase outlet of film absorber.
Above-mentioned film absorber adopts the design of automatic on-line backwash and cleaning, pollutes to control and to alleviate film.Automatic control system adopts seawater A forward and backwash timing alternate run to control pattern, to prevent the dirty stifled membrane component water inlet end face of mud and biological attachment.Like Fig. 8 and box film absorber shown in Figure 9 is example, and to be seawater flow to from 101,102 forward mode of operation, and through feed pipe 111, curtain type membrane element end socket 112, hollow-fibre membrane 13 mesopores of the every group of membrane component of flowing through from top to bottom flow out from 107,108; To be seawater flow to from 103,104 the back-flushing operation pattern, and hollow-fibre membrane 13 mesopores of the every group of membrane component of flowing through from bottom to top flow out from 105,106.In the on-line cleaning operational mode shown in figure 10; Cleaning seawater B is flowed into by import 109; Through being installed in the flue dust of film cleaning part self-timing cleaning hollow-fibre membrane 113 surface depositions in the film absorber, to alleviate the pollution of flue dust doughnut film outer surface.Cleaning seawater and desulfurization seawater are concentrated and are entered the aeration tank, carry out aeration and handle, and the pH value is recovered the back and arranged the sea.
Below in conjunction with Fig. 2 a to Fig. 4 c the structure of pot type gas-liquid contact membranes absorber is described in further detail.
Pot type gas-liquid contact membranes absorber comprises pillar hydrophobic hollow fiber membrane component, a pot type housing 20 and flatly be arranged on the film cleaning part 14 in the said pot type housing 20; Shown in Fig. 4 a; Described pillar hydrophobic hollow fiber membrane components are organized in evenly loose being furnished with more in the said pot type housing 20; Shown in Fig. 2 a; Be provided with the support bar 5 parallel in every group of pillar hydrophobic hollow fiber membrane component with a central tube 3, the even pipe tap 8 of distribution some on the tube wall of said central tube 3, and these pipe tap 8 occupied region areas are greater than or equal the cross-sectional area of said central tube 3; Hollow-fibre membrane 1 in every group of pillar hydrophobic hollow fiber membrane component is rolled into column after through yarn 2 braidings; Two ends are with cast material 4 sealing casting; The hollow-fibre membrane 1 that said pillar hydrophobic hollow fiber membrane component is woven by yarn 2, central tube 3, support bar 5 adopt a cast molding of technology of these known, and be relatively independent between every group of pillar hydrophobic hollow fiber membrane component; For guaranteeing that hollow-fibre membrane 1 is evenly distributed in the surrounding space of central tube 3; Hollow-fibre membrane all is through the evenly accurate braiding of yarn 2; This structure helps gas and between hollow-fibre membrane, evenly distributes; Help the effective contact area maximization of gas-liquid, can prevent effectively that hollow-fibre membrane is combined into pencil.But want control centre's pipe 3 suitable with the diameter ratio of hollow-fibre membrane 1 cast; If both diameters than with inner diameter of centerpipe than hour; Hollow-fibre membrane tow around the central tube 3 can thicken so; Not only increase gas phase and flowed freely resistance, also reduced the absorption efficiency of unit doughnut membrane area.Therefore, central tube 3 and pillar membrane component diameter ratio are controlled between 1: 5 to 1: 2, the central tube diameter is that DN25 is between the DN80.
The structure of said film cleaning part is shown in Fig. 3 b; Comprise a plurality of scavenge pipes 15; The tube wall of said scavenge pipe 15 is provided with a plurality of nozzles 16; Said a plurality of scavenge pipe 15 is uniformly distributed with and integrated being connected on the said feed pipe 17 according to a determining deviation, can evenly spray cleaning agent to hollow-fibre membrane, realizes the cleaning to the doughnut film outer surface.
Shown in Fig. 2 b; The top and bottom of the said pillar hydrophobic hollow fiber membrane component of a part are provided with bilateral end socket 6,7; Shown in Fig. 2 c; The top and bottom of the said pillar hydrophobic hollow fiber of another part membrane component are provided with threeway end socket 9,10; Be the angle of 90 °, 135 ° and 135 ° or 90 °, 90 ° and 180 ° between each pipe end of threeway end socket respectively, the angle between said bilateral end socket and the threeway end socket pipe end can be adjusted according to connected mode between each pillar membrane component, is not unalterable.Fig. 2 d shows the end socket connected mode sketch map (circle that has sequence number 01-09 shown in the figure is not for representing the end socket of 9 groups of pillar membrane components) of 9 groups of pillar membrane components in the single-stage pot type film absorber:
01 and 07 is the threeway end socket: angle is 90 °, 135 °, 135 ° between the pipe end;
04 and 06 is the threeway end socket: angle is 90 °, 90 °, 180 ° between the pipe end;
02,05,08 is the bilateral end socket, and angle is 180 ° between the pipe end;
03 and 09 is the bilateral end socket, and angle is 90 ° between the pipe end;
01 and 07 respectively is provided with a free pipe end.
The bilateral end socket 7 of the bilateral end socket 6 of 9 groups of said pillar hydrophobic hollow fiber membrane component upper ends and the pipe end of threeway end socket 9, lower end and the pipe end of threeway end socket 10 interconnect assembling respectively and form path; As connecting among Fig. 2 d shown in the line between the relevant end socket (circle); The benefit that connects like this is the idle space that has reduced supply line, increases the film packed density; Wherein, the pillar hydrophobic hollow fiber membrane component that is provided with the threeway end socket all is positioned at the inwall place of said pot type housing 20; Shown in 100 among Fig. 2 d, the end socket of the top and bottom of the threeway end socket pillar membrane components of on the diagonal two groups symmetries all respectively is provided with a free pipe end, and all the other membrane component end socket pipe ends all form closed circuit, up and down totally 4 free pipe ends; Be provided with an aperture in the position that aligns with the free pipe end of each said threeway end socket on the wall of pot type housing 20; Promptly corresponding respectively 4 free pipe end places open 4 apertures; Said free pipe end stretches out housing from the aperture that aligns with it, these apertures are respectively as the liquid phase import and export; No matter be bilateral or threeway end socket with said pillar hydrophobic hollow fiber membrane component between can be to be threaded or the interlocking draw-in groove form such as is connected and all can.Shown in Fig. 2 b; Liquid phase A flow path is in the band bilateral end socket membrane component: the left side opening of bilateral end socket 7 flows into liquid phase A; A part is from top to bottom flowed through in the hollow-fibre membrane 1, and another part liquid phase A will be that the next one membrane component that is connected provides liquid phase A through the right opening of this bilateral end socket 7; At this moment, the bilateral end socket 6 of lower end will be received a last coupled liquid phase A who flows out in liquid phase A that membrane component flows out and this membrane component hollow-fibre membrane 1 that connects from left side opening and discharge through the right opening of this bilateral end socket 6 in the lump.Gas phase C is diffused into hollow-fibre membrane 1 outer surface after flowing out through the pipe tap on the central tube 38.
The water conservancy diversion that the top and bottom of the said pillar hydrophobic hollow fiber membrane component of many groups are provided with pillar hydrophobic hollow fiber membrane component supports or supporting construction; Shown in Fig. 3 a; Said water conservancy diversion supporting construction is one to be positioned at the water conservancy diversion gripper shoe 11 at said central tube top; Said water conservancy diversion gripper shoe 11 is provided with central tube locator card slotted eye 12 and gas phase pod apertures 13; Wherein, draw-in groove hole 12 can guarantee that not only gas phase C can flow into next stage pot type gas-liquid contact membranes absorber in the central tube 3, also plays the effect of sharing next stage pot type gas-liquid contact membranes absorber weight.The aperture that is uniformly distributed with on the water conservancy diversion gripper shoe 11 is the passage that flows to next stage pot type gas-liquid contact membranes absorber for the gas phase C that from the pipe tap 8 of central tube, flows out; Therefore this aperture is a gas phase pod apertures 13; The aperture of gas phase pod apertures 13 and quantity are wanted suitably; Whole gas phase pod apertures 13 occupied region areas are greater than on the said central tube the occupied region area of whole pipe tap 8 on the said water conservancy diversion gripper shoe, can circulate smoothly to realize big flow low-pressure gas phase.Shown in Fig. 3 c, said supporting construction is one to be positioned at the support base plate 18 of said central tube bottom, is provided with central tube locator card slotted eye 12 on the said support base plate 18 equally.Certainly, support on the base plate 18 with water conservancy diversion gripper shoe 11 on central tube locator card slotted eye 12 be that quantity equates, placement position is one to one, thereby plays effect fixing and support pillar hydrophobic hollow fiber membrane component.
Fig. 4 a is single-stage pot type film absorber (forward) operational mode sketch map, and wherein: A is a liquid phase, and B is a cleaning agent, and C is a gas phase, and 19 is the cleaning agent outlet, and 21 is the cleaning agent import, and 22,23,25,26 are the liquid phase import and export, and 24 is plug.Said single-stage pot type film absorber mainly comprises parts such as pillar hydrophobic hollow fiber membrane component, water conservancy diversion gripper shoe 11, base plate 18, film cleaning part 14, pot type housing 20; Pillar hydrophobic hollow fiber membrane component forms more than one group pillar membrane components through bilateral and the assembling of threeway end socket; Certainly; The structure of end socket can have various ways, includes but not limited to bilateral end socket described in the present invention and threeway end socket.Wherein pillar hydrophobic hollow fiber membrane component fills in the pot type housing 20 with certain film packed density.The hollow-fibre membrane cumulative volume that the pillar of group more than said film packed density is meant hydrophobic hollow fiber membrane components comprise accounts for the percentage of enclosure interior spatial volume, and its scope is 3%~50%.When pot type gas-liquid contact membranes absorber got into forward mode of operation, it was closed conditions that liquid phase imports and exports 25 and 26.A kind of liquid phase A gets into pot type film absorbers from import 22, imports and exports 23 from liquid phase behind the hollow-fibre membrane of the pillar hydrophobic hollow fiber membrane component that is connected through a plurality of bilaterals or threeway end socket of flowing through and flows out.Liquid phase A is from top to down through flowing through in the hollow-fibre membrane; After gas phase C then is pipe tap 8 outflows through central tube 3; Along hollow-fibre membrane outside towards on be diffused into the gas phase pod apertures 13 of water conservancy diversion gripper shoe 11 the aperture discharge; That is to say that the flow direction of gas-liquid phase is opposite in the tank body, well-known, to flow to when opposite both mass-transfer efficiency the highest when two-phase medium.Cleaning process is after cleaning agent B can regularly flow into film cleaning part 14 from cleaning agent import 21, to be sprayed at hollow-fibre membrane 1 surface and to wash, to prevent that impurity causes irreversible pollution to hollow-fibre membrane in the gas phase.Last cleaning agent B discharges from tank shell cleaning agent outlet 19.
Fig. 4 b shows single-stage pot type gas-liquid contact membranes absorber back-flushing operation pattern.The visible pillar hydrophobic hollow fiber membrane component of part of analysing and observe at Fig. 4 b fills in the pot type housing with certain film packed density through many groups pillar membrane component that bilateral and threeway end socket assemble.When pot type gas-liquid contact membranes absorber got into the recoil operational mode, it was closed conditions that liquid phase imports and exports 22 and 23.A kind of liquid phase A imports and exports 25 from liquid phase and gets into pot type gas-liquid contact membranes absorbers, imports and exports 26 from liquid phase behind the hollow-fibre membrane of the pillar hydrophobic hollow fiber membrane component that is connected through a plurality of bilaterals or threeway end socket of flowing through and flows out.The flow direction and the forward mode of operation of liquid phase in hollow-fibre membrane is opposite, and such operation can rinse out the impurity that sticks to the hollow-fibre membrane inner surface, prevents that long-play from causing irreversible pollution to hollow-fibre membrane.Cleaning agent B also is flowing into from cleaning agent import 21 and be sprayed at hollow-fibre membrane 1 surface and wash regularly, discharges from tank shell outlet 19 at last.
Multistage pot type gas-liquid contact membranes absorber is promptly by the parallel connection of multistage above-mentioned single-stage pot type gas-liquid contact membranes absorber and/or connect integrated; Wherein, the central tube of the pot type gas-liquid contact membranes absorber of series connection is communicated with each other, is provided with the water conservancy diversion supporting construction between the pot type gas-liquid contact membranes absorber of series connection in twos.In addition, the series connection of film absorber and/or parallel way have multiple, comprise the series-parallel mutual combination of water route connection in series-parallel and gas circuit, i.e. gas circuit when series connection, the series connection in water route is during with parallelly connected and gas circuit parallel connection, the series connection in water route and and the four kinds of basic modes of allying the communists.Said water route and gas circuit are respectively the paths of liquid phase and gas phase circulation.Can select the connected mode between the multistage pot type gas-liquid contact membranes absorber according to concrete working condition in a word.Fig. 4 c is one of numerous connected modes.
In multistage pot type gas-liquid contact membranes absorber, said water conservancy diversion supporting construction is the water conservancy diversion gripper shoe that is positioned at said central tube top, and said water conservancy diversion gripper shoe is provided with the gentle phase pod apertures of central tube locator card slotted eye; Said supporting construction is the support base plate that is set in place in each pot type gas-liquid contact membranes absorber bottom of lowermost layer, and said support base plate is provided with central tube locator card slotted eye.A kind of intergration model of two-stage series connection has been shown among Fig. 4 c, mainly is to have first order pot type gas-liquid contact membranes absorber I and second level pot type gas-liquid contact membranes absorber II assembled in series to form.Compare with single-stage pot type gas-liquid contact membranes absorber pattern, the main difference part is that the central tube top of first order pot type gas-liquid contact membranes absorber I does not have plug 24, just communicates between the central tube of two pot type gas-liquid contact membranes absorbers.The flow path of gas phase C is in the middle of to be a part of gas phase from the pipe tap 8 of the central tube of first order pot type gas-liquid contact membranes absorber I be diffused into the pot type housing of first order pot type gas-liquid contact membranes absorber I, and another part gas phase is diffused in the pot type housing of second level pot type gas-liquid contact membranes absorber II from its pipe tap 8 after flowing to the central tube of second level pot type gas-liquid contact membranes absorber II again; The gas phase C that is diffused in the pot type housing of first order pot type gas-liquid contact membranes absorber I can discharge through the back of flowing through in the pot type housing of second level pot type gas-liquid contact membranes absorber II of the gas phase pod apertures 13 on the water conservancy diversion gripper shoe 11.In addition, the cleaning agent that cleans operation is discharged through cleaning agent outlet 19.
Below in conjunction with Fig. 5 a to Figure 11 the structure of box gas-liquid contact membranes absorber is described in further detail.
Like Fig. 5 a-5c, Fig. 6 a and shown in Figure 8, the box gas-liquid contact membranes of a kind of novel low vapour lock absorber comprises casing 107, hollow fibre membrane component 124, is arranged on baffle plate 116 in the casing 117, is arranged on the film cleaning part on casing 117 tops.
Said hollow fibre membrane component is a sheet curtain formula hydrophobic hollow fiber membrane component 124; Said sheet curtain formula hydrophobic hollow fiber membrane component 124 be along vapor phase stream through direction and be that grid is network-like to be arranged in the described casing 117, multi-disc sheet curtain formula hydrophobic hollow fiber membrane component 124 is with certain film packed density, evenly be arranged in casing 117 inside.
Shown in Fig. 5 b and Fig. 5 c; Said sheet curtain formula hydrophobic hollow fiber membrane component 124 is made up of with the membrane component end socket 112 that is sealed in described doughnut diaphragm 123 upper/lower terminals of multi-disc the doughnut diaphragm 123 through braiding, and said membrane component end socket 112 is provided with and draws sap cavity 122; Said hollow fibre membrane component 124 is selected common curtain formula hollow fibre membrane component for use, and said common curtain formula hollow fibre membrane component comprises with the hollow-fibre membrane of arranging continuously of yarns and has the curtain type membrane element end socket 112 that draws sap cavity 122, shown in Fig. 5 b.Or select for use constriction to become curtain formula hollow fibre membrane component, said constriction becomes the curtain type membrane element to comprise the integrated form hollow-fibre membrane that multi beam is arranged side by side and has the curtain type membrane element end socket 112 that draws sap cavity 122, shown in Fig. 5 c.Described braiding or constriction become curtain formula hollow-fibre membrane to be meant that hollow-fibre membrane is arranged into loose curtain shape uniformly, and this structure helps hollow-fibre membrane and in the film absorber, evenly distributes, to realize the effective contact area maximization of gas-liquid.Between the every described sheet curtain formula hydrophobic hollow fiber membrane component 124 is relatively independent; The position that aligns respectively with a plurality of described membrane component end sockets 112 two ends in the said casing 117 is provided with feed pipe; Said membrane component end socket 112 two ends are connected to respectively on that feed pipe that aligns with it; On the wall of said casing 117; The position that aligns at the two ends with each feed pipe 111,118,119,120 is provided with an aperture; Casing 117 is stretched out at the two ends of said feed pipe from the aperture that aligns with it, thereby has formed the import/export 101,102,103,104,105,106,107,108 of a plurality of liquid phase entering/outflow pipelines.
Shown in Fig. 6 a; Said film cleaning part comprises that flatly being arranged on one in the casing 117 cleans feed pipe 114 and a plurality of scavenge pipes 115; Shown in Fig. 6 b; Be provided with the nozzle of some on the tube wall of said scavenge pipe 115 equably; A plurality of described scavenge pipes 115 are uniformly distributed with the spacing of certain optimization and concentrate and are connected on the described cleaning feed pipe 114, and level places casing 117 inside, and the height of said scavenge pipe 115 and the height of the concordant or said scavenge pipe 115 of the height of said membrane component end socket 112 are higher than the height of said membrane component end socket 112; Wall box is provided with and is used for the cleaning agent import 109 that cleaning agent flows to said film cleaning part, and cleaning agent outlet 110.The occupied region area of a plurality of said nozzle on the tube wall of each said scavenge pipe 115 is less than or equal to the cross-sectional area of said scavenge pipe 115.
As shown in Figure 7; The profile of said casing 117 can be the housing of square or cuboid; Because casing is the hexahedron of square or cuboid, therefore, six of said casing 117 face the wall and meditate be in twos one group be right opposite setting; Wherein one group opposite walls is openable box body wall, and remaining four sides box body wall is that sealing is provided with continuously.Casing 117 inner baffle plates 116 are the plate of a hollow; Said baffle plate 116 is vertical basically through direction with vapor phase stream; Said baffle plate 116 closely is arranged between the wall of the described sheet curtain of multi-disc formula hydrophobic hollow fiber membrane component 124 and said casing, said box be the housing of film absorber, therefore; Its inside should be provided with the baffle plate 116 of one-level at least; The setting of this baffle plate 116 can prevent gas from the spatial flow mistake beyond the membrane component, and purpose is to guarantee that gas evenly flows through the hollow-fibre membrane surface of membrane component, thereby makes effective contact area maximization of gas-liquid film osculating element.
Fig. 8 shows box gas-liquid contact membranes absorber (forward) operational mode, and liquid phase A is flowed into by the import 101 and 102 that a plurality of liquid phases get into pipeline, meanwhile, and with aperture 105,106 sealings; Flow through successively feed pipe 111 and 118, membrane component end socket 112, tube side, feed pipe 119 and 120 are by outlet 107 and 108 (seal this moment 103 and 104) outflow; Gas phase C along the curtain type membrane element that is the palisade network structure, flows through hollow-fibre membrane 113 outer surfaces perpendicular to the hollow-fibre membrane direction of principal axis by the shell side that forms in the casing one side inflow casing.Two kinds of (gas-liquid) fluids are directly contact, but is that medium carries out mass transfer with hydrophobic hollow fiber film 113.
Fig. 9 shows box gas-liquid contact membranes absorber back-flushing operation pattern.Liquid phase A is flowed into by import 105 and 106 (101 and 102 sealing), and the feed pipe 119 and 120 of flowing through successively, curtain type membrane element end socket 112, tube side, feed pipe 111 and 118 are flowed out by outlet 103 and 104 (107 and 108 sealing); Gas phase C through shell side, along the curtain type membrane element that is the palisade network structure, flows through hollow-fibre membrane 113 outer surfaces perpendicular to the hollow-fibre membrane direction of principal axis by casing one side inflow, and two kinds of not directly contacts of (gas-liquid) fluid are that medium carries out mass transfer with hollow-fibre membrane 113; Recoil pattern shown in Figure 9 comes down in the operational mode shown in Figure 8 liquid phase A at the inverted running of tube side; The purpose of alternate run of operation and recoil pattern is for realizing hollow-fibre membrane 113 inner surfaces and membrane component end socket 112 are drawn the flushing of sap cavity 122 water inlet end faces, slowing down the speed of hollow-fibre membrane inner surface pollution.
Figure 10 shows box gas-liquid contact membranes absorber on-line cleaning operational mode; Come down on the basis of Fig. 8 or (forward) shown in Figure 9 operation/back-flushing operation pattern; Open import 109; Cleaning agent B get into to clean feed pipe 114, by the scavenge pipe with a plurality of nozzles 115 cleaning fluid is sprayed to the doughnut film outer surface equably, when realizing on-line operation to the cleaning of doughnut film outer surface, the pollution speed of slowing down the doughnut film outer surface.
A kind of multistage integrated box gas-liquid contact membranes absorber can and/or be connected integrated by multistage above-mentioned box gas-liquid contact membranes absorber parallel connection.Figure 11 shows one of them concrete embodiment; Be to be connected with the box gas-liquid contact membranes absorber I of the first order after adopting partial box gas-liquid contact membranes absorber II half-twist, make in adjacent two box gas-liquid contact membranes absorbers sheet curtain formula hydrophobic hollow fiber membrane component arrangement mode along on the direction of gas phase C each other not vertically.State in realization on the basis of three kinds of patterns of box gas-liquid contact membranes absorber forward, backwash and cleaning operation, make the gas phase C film absorber (I to N level) of flowing through successively.
The integrated form of multistage integrated box gas-liquid contact membranes absorber can be that the organic assembling of the serial or parallel connection of multistage box film absorber connects, a kind of integrated form of tandem compound shown in Figure 11, but do not limit the present invention.
The running status of pot type among the present invention or box gas-liquid contact membranes absorber comprises (forward) operation, back-flushing operation and three kinds of patterns of on-line cleaning operation; Optimal design through automatic control; Can realize timing automatic switchover operation, can also utilize PLC control to realize three kinds of switchings between the pattern according to actual needs.No matter be that automation is switched or semi-automatic switching is the general knowledge that the present technique field is known, repeat no more.In like manner, in this membrane absorption method flue gas desulfurization with seawater device, also generally included the on-line detector device.
Embodiment 1:
Adopt membrane absorption method flue gas desulfurization with seawater technology as shown in Figure 1, the desulfurization core of its device is formed by 3 grades of box gas-liquid contact membranes absorber assembled in series shown in figure 11, adopts horizontal installation.Every grade of film absorber hollow-fibre membrane filling area 500m 2, film packed density about 9%; Adopt former seawater as absorption liquid, its electrical conductivity 47400 μ S/cm~51800 μ S/cm, pH value 7.45~8.22, temperature are normal temperature; Adopt actual coal-fired flue-gas, its SO 2Concentration 1000mg/Nm 3~1600mg/Nm 3, dust concentration 100mg/Nm 3, 130 ℃~150 ℃ of temperature get into before the film absorber, are cooled to below 50 ℃ through over-heat-exchanger.Control seawater total flow 5m 3/ h~25m 3/ h adopts the parallel way 3 grades of film absorbers of flowing through, the seawater hollow-fibre membrane mesopore of flowing through, liquid phase pressure 0.02MPa; Flue gas treating capacity 1000Nm 3Horizontal flow is through 3 grades of film absorbers successively for/h, flue gas, and the vertical fibers direction of principal axis flows through the hollow-fibre membrane outer wall, and flue gas is pressure 0.6kPa in the film absorber.Through after the stable operation, record the gaseous phase outlet flue gas SO of film absorber 2Concentration is at 20mg/Nm 3~100mg/Nm 3Between, desulfurization degree reaches 91.7%~98.5%, sea water after desulphurization pH value 3.1~5.7.Former seawater divides A, B two-way to get into the film absorber; A road seawater gets into tube side and carries out desulfurization; B road seawater gets into and is installed in the film cleaning part between the film absorber shell side; Automatic control system employing forward/back-flushing operation pattern alternate run regularly sprays the technology that seawater cleans to film outer surface through the film cleaning part, with the film pollution of control and minimizing gas phase and liquid phase.Clean the concentrated aeration tank that enters of seawater and desulfurization seawater, handled 20 minutes, the back up to standard discharging of pH value through aeration.
Embodiment 2:
Adopt technology, device and the absorption liquid identical with the foregoing description 1, flue gas is SO 2Concentration is 2860mg/Nm 3And 4290mg/Nm 3The actual coal-fired flue-gas of high concentration, the control seawater flow is 15m 3/ h, the pH value is 8.20~8.51, the flue gas treating capacity is at 500Nm 3/ h~1300Nm 3In/h the scope, corresponding concentration is 2860mg/Nm 3Flue gas, desulfurization degree 97.7%~88.5%, sea water after desulphurization pH value 3.3~5.5; Corresponding concentration is 4290mg/m 3Flue gas, flue gas treating capacity≤1000Nm 3Under/h the situation, desulfurization degree 97.1%~90.6%, sea water after desulphurization pH value 2.7~5.0.Flue gas SO 2Concentration is at 1000mg/Nm 3~4290mg/Nm 3Fluctuation in the scope, flue gas treating capacity≤1000Nm 3/ h, desulfurization degree all reaches more than 90%.It is all identical with embodiment 1 that the film of gas phase and liquid phase pollutes the post processing of control and cleaning seawater and desulfurization seawater.
Although invention has been described for top combination figure; But the present invention is not limited to the above-mentioned specific embodiment, and the above-mentioned specific embodiment only is schematically, rather than restrictive; Those of ordinary skill in the art is under enlightenment of the present invention; Under the situation that does not break away from aim of the present invention, can also make a lot of distortion, these all belong within the protection of the present invention.

Claims (10)

1. membrane absorption method flue gas desulfurization with seawater device, the sea water preprocessing equipment (3) that comprise one-level film absorber (1) at least, links to each other successively and sea water pump (4), the heat exchanger (8) and the ventilation apparatus that link to each other successively; The liquid phase import of said film absorber (1) links to each other with said sea water pump (4), and the gas phase import of said film absorber (1) links to each other with said ventilation apparatus;
It is characterized in that:
The liquid phase outlet of said film absorber (1) links to each other with an aeration tank (5);
Said ventilation apparatus adopts booster fan (9);
Said film absorber (1) adopts a kind of in box gas-liquid contact membranes absorber and the pot type gas-liquid contact membranes absorber, wherein:
Said box gas-liquid contact membranes absorber: comprise hollow fibre membrane component, a casing, be arranged on the baffle plate in the casing and be arranged on the film cleaning part on casing top; Form a film absorber shell side between the wall of said hollow fibre membrane component and casing;
Said hollow fibre membrane component is a sheet curtain formula hydrophobic hollow fiber membrane component;
Be the network-like described sheet curtain of the multi-disc formula hydrophobic hollow fiber membrane component that is furnished with of grid along vapor phase stream through direction in the said casing;
Said sheet curtain formula hydrophobic hollow fiber membrane component is made up of with the membrane component end socket that is sealed in the described sheet curtain of multi-disc formula hydrophobic hollow fiber diaphragm upper/lower terminal the doughnut diaphragm through braiding, and said membrane component end socket is provided with and draws sap cavity;
Relatively independent between the every described sheet curtain formula hydrophobic hollow fiber membrane component; Be provided with feed pipe with a plurality of described membrane component end sockets two ends align respectively; Said membrane component end socket two ends are connected to respectively on the feed pipe that aligns with it; The position that aligns at the two ends with each feed pipe on the wall of said casing is provided with an aperture, and casing is stretched out in the two ends of said feed pipe from the aperture that aligns with it;
Said baffle plate is the plate of a hollow, and said baffle plate is vertical basically through direction with vapor phase stream, and said baffle plate closely is arranged between the described sheet curtain of multi-disc formula hydrophobic hollow fiber membrane component and the said casing;
Said film cleaning part comprises that flatly being arranged on one in the casing cleans feed pipe and a plurality of scavenge pipe, is provided with a plurality of nozzles on the tube wall of said scavenge pipe equably, and a plurality of described scavenge pipes are connected on the described cleaning feed pipe; Said pot type gas-liquid contact membranes absorber: comprise hollow fibre membrane component, a pot type housing and flatly be arranged on the film cleaning part in the said pot type housing; Form a film absorber shell side between the wall of said hollow fibre membrane component and tank body;
Said hollow fibre membrane component is a pillar hydrophobic hollow fiber membrane component;
Evenly be furnished with the described pillar hydrophobic hollow fiber membrane component of many groups in the said pot type housing; Be provided with the support bar parallel in every group of pillar hydrophobic hollow fiber membrane component with a central tube; The hole of even distribution some on the tube wall of said central tube; The occupied region area in all holes is greater than or equals the cross-sectional area of said central tube, and the top of said central tube is provided with plug;
Hollow-fibre membrane in every group of pillar hydrophobic hollow fiber membrane component is rolled into column through after the yarns, the sealed at both ends casting; Relatively independent between every group of pillar hydrophobic hollow fiber membrane component;
The top and bottom of the said pillar hydrophobic hollow fiber membrane component of a part are provided with the bilateral end socket, and the top and bottom of the said pillar hydrophobic hollow fiber of another part membrane component are provided with the threeway end socket; The pipe end of the bilateral end socket on the said pillar hydrophobic hollow fiber membrane component of many groups and the pipe end of threeway end socket interconnect assembling respectively and form path on same horizontal plane; The pillar hydrophobic hollow fiber membrane component that is provided with the threeway end socket all is positioned at the inwall place of said pot type housing; Wherein, the end socket of the top and bottom of the threeway end socket pillar membrane component of the symmetry of two groups on the diagonal all respectively is provided with a free pipe end; Be provided with an aperture in the position that aligns with each free pipe end on the wall of pot type housing, said free pipe end stretches out housing from the aperture that aligns with it;
The water conservancy diversion that the top and bottom of the said pillar hydrophobic hollow fiber membrane component of many groups are provided with pillar hydrophobic hollow fiber membrane component supports or supporting construction; Said water conservancy diversion supporting construction includes a plurality of gas phase pod apertures;
Said film cleaning part comprises that flatly being arranged on one in the tank body cleans feed pipe and a plurality of scavenge pipe, and the tube wall of said scavenge pipe is provided with a plurality of nozzles, and said a plurality of scavenge pipes are integrated and connected to said feed pipe.
2. according to the said membrane absorption method flue gas desulfurization with seawater of claim 1 device; It is characterized in that; Said hollow fibre membrane component; Its membrane material is selected from polytetrafluoroethylene (PTFE), Kynoar, polyvinyl chloride, polysulfones, polyether sulfone, polyether sulphone, polyethylene, polypropylene, polyester, silicon rubber, one or more polyblends or compound membrane material.
3. according to the said membrane absorption method flue gas desulfurization with seawater of claim 1 device; It is characterized in that, said hollow fibre membrane component, its perforated membrane maximum diameter of hole scope is 0.01 μ m~2.0 μ m; Wall thickness range is 20 μ m~200 μ m, and porosity ranges is 30%~80%; Hollow-fibre membrane average diameter scope is 100 μ m~3000 μ m.
4. according to the said membrane absorption method flue gas desulfurization with seawater of claim 1 device, it is characterized in that the percentage between hollow-fibre membrane cumulative volume that said hollow fibre membrane component comprised and the said box or pot type vome of shell is 3%~50%.
5. according to the said membrane absorption method flue gas desulfurization with seawater of claim 1 device, it is characterized in that the occupied region area of nozzle in the said film cleaning part is less than or equal to the cross-sectional area of scavenge pipe.
6. according to the said membrane absorption method flue gas desulfurization with seawater of claim 1 device; It is characterized in that; The water conservancy diversion supporting construction is one to be positioned at the water conservancy diversion gripper shoe at said central tube top in the said pot type gas-liquid contact membranes absorber, and said water conservancy diversion gripper shoe is provided with the gentle phase pod apertures of central tube locator card slotted eye; Said supporting construction is one to be positioned at the support base plate of said central tube bottom, and said support base plate is provided with central tube locator card slotted eye; The occupied region area of gas phase pod apertures is greater than total hole area of said central tube cinclides on the said water conservancy diversion gripper shoe.
7. a membrane absorption method flue gas desulfurization with seawater technology is characterized in that, the process of utilizing membrane absorption method flue gas desulfurization with seawater device as claimed in claim 1 to carry out flue gas desulfurization is:
Flue gas (7) is sent into film absorber shell side through booster fan (9) after heat exchanger (8) adopts the cooled with seawater cooling;
Get into film absorber tube side as the desulfurization absorption liquid through the pretreated seawater of sea water preprocessing equipment (3) (2) through sea water pump (4);
Gas-liquid two-phase forms reaction interface at the micropore place of hollow-fibre membrane, and the reaction of SO2 and seawater generates sulphite in the flue gas;
Flue gas after the desulfurization is discharged from the gaseous phase outlet of said film absorber (1); Meanwhile, the seawater that has sulphite is the solid sulphur of (5) aeration through the aeration tank, and (6) are discharged in its pH value back up to standard.
8. according to claim 7 membrane absorption method flue gas desulfurization with seawater technology; It is characterized in that; Said seawater is meant any in the concentrated seawater of seawater, seawater circulation cooling and embrane method desalinization discharging of former seawater, seawater direct current cooling discharging; Its conductivity range is 30000 μ S/cm~80000 μ S/cm, and its pH value is controlled at more than 7.5.
9. according to claim 7 membrane absorption method flue gas desulfurization with seawater technology, it is characterized in that said flue gas is meant through the coal-fired flue-gas after the dedusting and/or contains SO 2Industrial waste gas, SO wherein 2Concentration range 50mg/Nm 3~5000mg/Nm 3, its pressure limit 0KPa~2.0KPa in the film absorber.
10. according to claim 7 membrane absorption method flue gas desulfurization with seawater technology, it is characterized in that said film absorber adopts automatic on-line backwash and cleaning, control and alleviate film and pollute.
CN 201010572971 2010-12-05 2010-12-05 Device for desulfurizing flue gas by seawater through membrane absorption and its process CN102485320B (en)

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CN103331095A (en) * 2013-07-16 2013-10-02 国家海洋局天津海水淡化与综合利用研究所 Simultaneous desulphurization and denitration device for seawater smoke with membrane absorption method, as well as process of device
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