CN214345523U - Two-stage absorption membrane method seawater flue gas desulfurization device - Google Patents
Two-stage absorption membrane method seawater flue gas desulfurization device Download PDFInfo
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- CN214345523U CN214345523U CN202022812717.XU CN202022812717U CN214345523U CN 214345523 U CN214345523 U CN 214345523U CN 202022812717 U CN202022812717 U CN 202022812717U CN 214345523 U CN214345523 U CN 214345523U
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- 239000012528 membrane Substances 0.000 title claims abstract description 169
- 239000013535 sea water Substances 0.000 title claims abstract description 130
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 110
- 239000003546 flue gas Substances 0.000 title claims abstract description 110
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 39
- 230000023556 desulfurization Effects 0.000 title claims abstract description 37
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 33
- 238000005273 aeration Methods 0.000 claims abstract description 56
- 239000000779 smoke Substances 0.000 claims description 9
- 239000000919 ceramic Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 7
- 238000009434 installation Methods 0.000 abstract description 3
- 230000001737 promoting effect Effects 0.000 abstract 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 14
- 239000007789 gas Substances 0.000 description 10
- 230000008569 process Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 239000012071 phase Substances 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 239000002253 acid Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 241000282414 Homo sapiens Species 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000005465 channeling Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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- 230000005514 two-phase flow Effects 0.000 description 1
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Abstract
The utility model discloses a two-stage absorption membrane method seawater flue gas desulfurization device. The device comprises a flue gas pretreatment device, a membrane component, a seawater pool, a seawater pump, an aeration fan and an aeration tank; the membrane component comprises a first-stage membrane component and a second-stage membrane component; the inlet end of the flue gas pretreatment device is connected with the raw flue gas system, and the outlet end of the flue gas pretreatment device is connected with the first-stage membrane component; the first-stage membrane component is respectively connected with the second-stage membrane component and the aeration tank; the aeration fan is connected with the aeration tank; the aeration tank is provided with a seawater outlet; the secondary membrane component is connected with the seawater pool; the sea water pump is arranged on a connecting pipeline between the secondary membrane module and the sea water pool. The utility model has the advantages of flexible installation, small occupied area, simple and convenient operation, capability of promoting desulfurization efficiency and saving energy consumption along with a flue gas volume adjusting device.
Description
Technical Field
The utility model relates to a two-stage absorption membrane method seawater flue gas desulfurization device.
Background
Sulfur dioxide is a main atmospheric pollutant and is directly discharged into the atmosphere, which can affect the health of human beings, in order to reduce the discharge amount of sulfur dioxide, the government of China always puts a stricter policy on limiting the discharge amount of sulfur dioxide, and proposes to put forward 'ultra-clean discharge' in the national region in 2015 for 12 months. In order to respond to increasingly stringent environmental protection policies and to relieve environmental pressure, it is imperative to continuously improve the existing desulfurization environmental protection technologies and to develop new environmental protection technologies.
Compared with the traditional limestone-gypsum and ammonia desulphurization technology and other desulphurization technologies, the seawater desulphurization technology has the obvious advantages of high desulphurization efficiency, low operation cost, less investment, simple and reliable system, no additive, no by-product and the like, and the adoption of seawater desulphurization is a better choice for the seaside power plant and the ship. The traditional seawater desulfurization process is generally carried out in a packed tower, a bubble tower and a spray tower, and the conventional method generally has the problems of high investment cost, large occupied area, complex equipment, difficult operation and the like.
Therefore, there is a need to develop a seawater flue gas desulfurization device with small floor space, simple equipment operation and energy saving.
Disclosure of Invention
The utility model aims at providing a embrane method sea water flue gas desulphurization unit is absorbed in second grade, the installation is nimble, and area is little, and is easy and simple to handle, can promote desulfurization efficiency, practice thrift the energy consumption along with flue gas volume adjusting device.
In order to realize the purpose, the technical scheme of the utility model is that: a sea water flue gas desulfurization device adopting a two-stage absorption membrane method is characterized in that: comprises a flue gas pretreatment device, a membrane component, a seawater pool, a seawater pump, an aeration fan and an aeration tank;
the membrane component comprises a first-stage membrane component and a second-stage membrane component;
the inlet end of the flue gas pretreatment device is connected with the raw flue gas system, and the outlet end of the flue gas pretreatment device is connected with the first-stage membrane component;
the first-stage membrane component is respectively connected with the second-stage membrane component and the aeration tank; the aeration fan is connected with the aeration tank; the aeration tank is provided with a seawater outlet;
the secondary membrane component is connected with the seawater pool; the sea water pump is arranged on a connecting pipeline between the secondary membrane module and the sea water pool.
In the above technical scheme, the primary membrane module comprises a primary flue gas inlet, a primary flue gas outlet, a primary seawater inlet and a primary seawater outlet;
the first-stage flue gas inlet and the first-stage flue gas outlet are both arranged on the side wall of the first-stage membrane component; wherein, the first-stage flue gas inlet is arranged at the upper part of the first-stage membrane component, and the first-stage flue gas outlet is arranged at the lower part of the first-stage membrane component;
the first-stage seawater inlet is arranged at the lower end of the first-stage membrane component; the first-stage seawater outlet is arranged at the upper end of the first-stage membrane component;
the first-stage flue gas inlet is connected with the outlet end of the flue gas pretreatment device;
the first-stage seawater outlet is connected with the upper end of the aeration tank.
In the technical scheme, the secondary membrane component comprises a secondary flue gas inlet, a secondary flue gas outlet, a secondary seawater inlet and a secondary seawater outlet;
the secondary flue gas inlet and the secondary flue gas outlet are both arranged on the side wall of the secondary membrane component; wherein, the secondary flue gas inlet is arranged at the upper part of the secondary membrane component, and the secondary flue gas outlet is arranged at the lower part of the secondary membrane component;
the second-stage seawater inlet is arranged at the lower end of the second-stage membrane component; the second-stage seawater outlet is arranged at the upper end of the second-stage membrane component;
the second-stage seawater inlet is connected with the seawater pool; a seawater pump is arranged between the second-stage seawater inlet and the seawater pool;
the second-stage seawater outlet is connected with the first-stage seawater inlet;
the second-level smoke inlet is connected with the first-level smoke outlet.
In the technical scheme, a plurality of aeration nozzles are arranged in the aeration tank; the aeration nozzle is connected with the aeration fan.
In the technical scheme, the porous membranes in the first-stage membrane component and the second-stage membrane component are hydrophilic tubular porous ceramic membranes; wherein the porous membrane has a water drop contact angle of 10 to 50 deg.
The utility model has the advantages of as follows:
(1) the utility model adopts the membrane absorption device, the gas phase and the liquid phase flow in the shell pass and the tube pass of the membrane contactor independently, the gas phase and the liquid phase are contacted on the outer surface of the membrane, the operation can be flexibly carried out without mutual interference, and the problems of flooding, liquid leakage, entrainment, channeling, wall flow, large power consumption and the like in the traditional absorption tower are effectively avoided;
(2) the middle membrane absorption device of the utility model adopts the ceramic membrane as the component material, has high gas permeation flux, natural dust pollution resistance and self-cleaning capability, and has better load capacity for high-temperature and high-pressure flue gas and alkaline absorbent;
(3) seawater is adopted as a desulfurization absorbent in desulfurization projects of seaside power plants, ships, islands and the like, and compared with the traditional limestone-gypsum method, ammonia method, sodium-alkali method and the like, the utility model can greatly reduce the cost of the absorption liquid;
(4) the utility model reasonably designs the process flow, adopts a secondary membrane absorption device in the whole flow, and the raw flue gas firstly enters a primary membrane absorption component and then enters a secondary membrane absorption component; fresh seawater firstly enters the second-stage membrane component and then enters the first-stage membrane component; the desulfurization efficiency can be greatly improved, the consumption of seawater is reduced, and the energy consumption is saved; the problem of large energy consumption of the traditional desulfurization method is solved;
(5) the whole system of the utility model can be separated and integrated, has compact structure and high integration, and is suitable for the upgrading and reconstruction of desulfurization processes of middle and small coal-fired thermal power plants, ships and other flue gas generating equipment; the utility model has the advantages of flexible installation, small occupied area, capability of adjusting the device along with the amount of flue gas, high desulfurization efficiency and the like, and can be skid-mounted in a place with strict space area requirement; the utility model has good application prospect for occasions with abundant seawater resources, such as seaside power plants, ships and the like, and can be popularized on a large scale;
(6) the utility model discloses can adjust the number of sea water quantity and membrane module the inside at any time according to flue gas sulfur dioxide concentration and flue gas flow, the operating parameter is nimble, adapts to the change of operating condition flue gas, but maximum reduction energy consumption.
The utility model couples the characteristics of the traditional absorption and membrane separation technology, and has the outstanding advantages of flexible operation, compact structure, high integration degree and the like; the utility model provides a combine together natural seawater and membrane absorption method technique, develop a sea water desulphurization unit based on embrane method, through the double-phase pressure difference of control gas-liquid, the micropore that utilizes the membrane is that the gas-liquid is double-phase to flow intraductal and tube respectively, does not take place the alternate mixing, and two-phase flow mutual noninterference has avoided flooding in the traditional absorption tower effectively, weeping, fog foam to smuggle secretly, the furrow, wall flow, the great scheduling problem of power consumption.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
E in FIG. 1 represents that the desulfurized seawater treated in the aeration tank is discharged into the sea; f represents that the clean flue gas treated by the secondary membrane module is discharged into the air through a secondary flue gas outlet.
In the figure, 1-a flue gas pretreatment device, 2-a membrane component, 2.1-a first-stage membrane component, 2.11-a first-stage flue gas inlet, 2.12-a first-stage flue gas outlet, 2.13-a first-stage seawater inlet, 2.14-a first-stage seawater outlet, 2.2-a second-stage membrane component, 2.21-a second-stage flue gas inlet, 2.22-a second-stage flue gas outlet, 2.23-a second-stage seawater inlet, 2.24-a second-stage seawater outlet, 3-a seawater pool, 4-a seawater pump, 5-an aeration fan, 6-an aeration pool, 6.1-an aeration nozzle and 7-a seawater outlet.
Detailed Description
The following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings, which are not intended to limit the present invention, but are merely exemplary. While the advantages of the invention will be clear and readily appreciated by the description.
With reference to the accompanying drawings: a seawater flue gas desulfurization device adopting a two-stage absorption membrane method comprises a flue gas pretreatment device 1, a membrane component 2, a seawater pool 3, a seawater pump 4, an aeration fan 5 and an aeration tank 6;
the membrane component 2 comprises a first-stage membrane component 2.1 and a second-stage membrane component 2.2; the device of the utility model has compact structure, can be designed in a split way (the first-stage membrane component 2.1 and the second-stage membrane component 2.2 can be combined for use or can be used independently), can be integrated for skid mounting, and can adapt to different occasions;
the inlet end of the flue gas pretreatment device 1 is connected with a raw flue gas system, and the outlet end of the flue gas pretreatment device is connected with a first-stage membrane module 2.1; the original flue gas is dedusted by the flue gas pretreatment device 1 and then introduced into the primary membrane module system, so that the influence of impurities in the flue gas on the subsequent membrane module can be avoided;
the first-stage membrane component 2.1 is respectively connected with the second-stage membrane component 2.2 and the aeration tank 6; the flue gas desulfurization process is carried out in two stages, the flue gas enters a first-stage membrane component tube system firstly, and then enters a second-stage membrane component tube system, and the desulfurization is absorbed and desulfurized in the second stage, so that the desulfurization efficiency can be effectively improved, and the energy consumption is reduced;
the aeration fan 5 is connected with the aeration tank 6; the aeration tank 6 is provided with a seawater outlet 7, and the desulfurized seawater treated by the aeration tank 6 is discharged into the sea from the seawater outlet 7;
the secondary membrane component 2.2 is connected with the seawater pool 3; fresh seawater enters a pipe of the secondary membrane module to absorb sulfur dioxide in the secondary flue gas; then enters the tube of the first-stage membrane component to absorb the sulfur dioxide in the original flue gas; under the condition of the same amount of seawater, the secondary membrane absorption device can effectively improve the desulfurization efficiency and save energy consumption;
the seawater pump 4 is arranged on a connecting pipeline between the secondary membrane module 2.2 and the seawater pool 3; the seawater pump 4 is used for conveying fresh seawater in the seawater pool 3 to the secondary membrane module 2.2 and the primary membrane module 2.1.
Further, the primary membrane module 2.1 comprises a primary flue gas inlet 2.11, a primary flue gas outlet 2.12, a primary seawater inlet 2.13 and a primary seawater outlet 2.14;
the primary flue gas inlet 2.11 and the primary flue gas outlet 2.12 are both arranged on the side wall of the primary membrane module 2.1; wherein, the first-stage flue gas inlet 2.11 is arranged at the upper part of the first-stage membrane module 2.1, and the first-stage flue gas outlet 2.12 is arranged at the lower part of the first-stage membrane module 2.1;
a primary seawater inlet 2.13 is arranged at the lower end of the primary membrane component 2.1; a first-stage seawater outlet 2.14 is arranged at the upper end of the first-stage membrane component 2.1;
the primary flue gas inlet 2.11 is connected with the outlet end of the flue gas pretreatment device 1;
the first-stage seawater outlet 2.14 is connected with the upper end of the aeration tank 6; the pH of the desulfurized seawater discharged from the primary seawater outlet 2.14 is restored by the aeration tank 6.
Further, the secondary membrane module 2.2 comprises a secondary flue gas inlet 2.21, a secondary flue gas outlet 2.22, a secondary seawater inlet 2.23 and a secondary seawater outlet 2.24;
the secondary flue gas inlet 2.21 and the secondary flue gas outlet 2.22 are both arranged on the side wall of the secondary membrane module 2.2; wherein, the secondary flue gas inlet 2.21 is arranged at the upper part of the secondary membrane module 2.2, and the secondary flue gas outlet 2.22 is arranged at the lower part of the secondary membrane module 2.2;
the second-stage seawater inlet 2.23 is arranged at the lower end of the second-stage membrane component 2.2; the secondary seawater outlet 2.24 is arranged at the upper end of the secondary membrane component 2.2;
the second-stage seawater inlet 2.23 is connected with the seawater pool 3; a seawater pump 4 is arranged between the second-stage seawater inlet 2.23 and the seawater pool 3;
the second-stage seawater outlet 2.24 is connected with the first-stage seawater inlet 2.13;
the secondary flue gas inlet 2.21 is connected with the primary flue gas outlet 2.12; raw flue gas firstly enters a primary membrane absorption assembly and then enters a secondary membrane absorption assembly; fresh seawater firstly enters the second-stage membrane component and then enters the first-stage membrane component; the desulfurization efficiency can be greatly improved, the consumption of seawater is reduced, and the energy consumption is saved;
the second-stage smoke outlet 2.22 is a clean smoke discharge outlet, and the clean smoke treated by the second-stage membrane module 2.2 is discharged through the second-stage smoke outlet 2.22.
Furthermore, a plurality of aeration nozzles 6.1 are arranged in the aeration tank 6, and the aeration nozzles 6.1 are arranged at the lower part of the aeration tank 6; the aeration nozzle 6.1 is used for spraying gas in the aeration tank 6 to recover the pH value of the desulfurized seawater;
the aeration nozzle 6.1 is connected with an aeration fan 5; the aeration fan 5 is used for providing an air source for the aeration nozzle 6.1.
Further, the first-stage membrane module 2.1 and the second-stage membrane module 2.2 both comprise a shell side, a tube side and a porous membrane; wherein, the porous membrane is a hydrophilic ceramic membrane; almost all SO can be removed by using a hydrophilic membrane as a membrane in a membrane absorption device (i.e. a membrane module)2Hardly absorb CO2Avoiding CO in the acid seawater after desulfurization2The increase of the pH value is not beneficial to the recovery of the pH value of the seawater in the subsequent aeration treatment process.
The porous membranes in the first-stage membrane component 2.1 and the second-stage membrane component 2.2 are hydrophilic ceramic membranes; almost all SO can be removed by using a hydrophilic membrane as a membrane in a membrane absorption device (i.e. a membrane module)2Hardly absorb CO2Avoiding CO in the acid seawater after desulfurization2The increase of the pH value is not beneficial to the recovery of the pH value of the seawater in the subsequent aeration treatment process; the ceramic membrane has high gas permeation flux, natural dust pollution resistance and self-cleaning capability, and better load capacity on high-temperature and high-pressure flue gas and an alkaline absorbent;
wherein the water drop contact angle of the porous membrane is 10-50 degrees; as the membrane absorption device, the porous membrane has better hydrophilicity (the hydrophilicity can be understood as that the water drop contact angle ranges from 10 to 50 degrees), the porous membrane in the utility model can adopt a tubular porous ceramic membrane, so that absorption liquid passes through the tube side, gas passes through the shell side, smoke and absorbent respectively flow in a two-phase parallel countercurrent mode on the shell side and the tube side of the membrane contactor, and the absorption of the gas occurs on the surface of the membrane.
The desulfurization method of the seawater flue gas desulfurization device adopting the two-stage absorption membrane method comprises the following steps,
the method comprises the following steps: the original flue gas is dedusted by the flue gas pretreatment device 1, and the flue gas pretreatment device 1 is firstly adopted to pretreat the gas, mainly used for removing some particulate matters in the gas, so that the normal operation of the subsequent porous membrane can be effectively protected; the pretreatment is dust removal treatment, and can be performed in a filtering mode, an electrostatic adsorption mode and other modes, so that the influence of impurities in the flue gas on the subsequent membrane module 2 can be avoided;
step two: fresh seawater firstly enters the secondary membrane component 2.2 and then enters the primary membrane component 2.1 through the secondary membrane component 2.2;
the primary membrane component 2.1 carries out primary desulfurization on the flue gas after dust removal, and the flue gas after primary desulfurization enters the secondary membrane component 2.2;
the secondary membrane component 2.2 carries out secondary desulfurization on the flue gas entering the secondary membrane component, and the clean flue gas is discharged after the flue gas is desulfurized by the secondary membrane component 2.2; the utility model discloses an in the processing procedure, at first need adopt hydrophilic ceramic membrane to absorb gas, adopt natural sea water as absorption liquid mainly in the middle of this process, the utility model discloses creatively adopt hydrophilic porous membrane to SO in foretell membrane absorption process2Performing selective absorption, wherein the hydrophilic porous membrane is opposite to SO2The selective absorbability is higher; after absorption treatment, SO2Can penetrate hydrophilic membrane layer to generate Na2SO3Inorganic salts can be directly discharged after subsequent oxidation, concentration and purification, and can also be reused as recycled salts;
step three: the desulfurized seawater discharged from the first-stage membrane module 2.1 enters an aeration tank 6 from the top; the aeration tank 6 recovers the pH value of the desulfurized seawater, and ensures that the desulfurized seawater with the pH value of more than 6.8 can be discharged into the sea according to the standard and standard requirements of seawater quality; the seawater treated by the aeration tank 6 is discharged into the sea from a seawater discharge outlet 7.
In order to illustrate more clearly the utility model discloses a second grade absorb embrane method sea water flue gas desulfurization device compare the advantage that has with prior art, the staff has carried out the contrast with these two kinds of technical scheme, its contrast result is as follows:
according to the table, the sea water flue gas desulfurization device of the second grade absorption film method is compared with the prior art, the investment cost is low, the floor area is small, the desulfurization efficiency is high, the desulfurization effect is good, the desulfurization use cost is low, the system resistance is smaller, and the processing scale can be adjusted according to the actual use condition.
Other parts not described belong to the prior art.
Claims (5)
1. A sea water flue gas desulfurization device adopting a two-stage absorption membrane method is characterized in that: comprises a flue gas pretreatment device (1), a membrane component (2), a seawater pool (3), a seawater pump (4), an aeration fan (5) and an aeration tank (6);
the membrane component (2) comprises a first-stage membrane component (2.1) and a second-stage membrane component (2.2);
the inlet end of the flue gas pretreatment device (1) is connected with a raw flue gas system, and the outlet end of the flue gas pretreatment device is connected with the first-stage membrane component (2.1);
the first-stage membrane component (2.1) is respectively connected with the second-stage membrane component (2.2) and the aeration tank (6); the aeration fan (5) is connected with the aeration tank (6); a seawater outlet (7) is arranged on the aeration tank (6);
the secondary membrane component (2.2) is connected with the seawater pool (3); the seawater pump (4) is arranged on a connecting pipeline between the secondary membrane module (2.2) and the seawater pool (3).
2. The seawater flue gas desulfurization device by the two-stage absorption membrane method according to claim 1, characterized in that: the primary membrane component (2.1) comprises a primary flue gas inlet (2.11), a primary flue gas outlet (2.12), a primary seawater inlet (2.13) and a primary seawater outlet (2.14);
the primary flue gas inlet (2.11) and the primary flue gas outlet (2.12) are both arranged on the side wall of the primary membrane component (2.1); wherein, the first-stage flue gas inlet (2.11) is arranged at the upper part of the first-stage membrane component (2.1), and the first-stage flue gas outlet (2.12) is arranged at the lower part of the first-stage membrane component (2.1);
the primary seawater inlet (2.13) is arranged at the lower end of the primary membrane component (2.1); the primary seawater outlet (2.14) is arranged at the upper end of the primary membrane component (2.1);
the primary flue gas inlet (2.11) is connected with the outlet end of the flue gas pretreatment device (1);
the first-stage seawater outlet (2.14) is connected with the upper end of the aeration tank (6).
3. The seawater flue gas desulfurization device by the two-stage absorption membrane method according to claim 2, characterized in that: the secondary membrane component (2.2) comprises a secondary flue gas inlet (2.21), a secondary flue gas outlet (2.22), a secondary seawater inlet (2.23) and a secondary seawater outlet (2.24);
the secondary flue gas inlet (2.21) and the secondary flue gas outlet (2.22) are both arranged on the side wall of the secondary membrane component (2.2); wherein, the secondary flue gas inlet (2.21) is arranged at the upper part of the secondary membrane component (2.2), and the secondary flue gas outlet (2.22) is arranged at the lower part of the secondary membrane component (2.2);
the secondary seawater inlet (2.23) is arranged at the lower end of the secondary membrane component (2.2); the secondary seawater outlet (2.24) is arranged at the upper end of the secondary membrane component (2.2);
the secondary seawater inlet (2.23) is connected with the seawater pool (3); a seawater pump (4) is arranged between the secondary seawater inlet (2.23) and the seawater pool (3);
the secondary seawater outlet (2.24) is connected with the primary seawater inlet (2.13);
the second-level smoke inlet (2.21) is connected with the first-level smoke outlet (2.12).
4. The seawater flue gas desulfurization device by the two-stage absorption membrane method according to claim 3, characterized in that: a plurality of aeration nozzles (6.1) are arranged in the aeration tank (6); the aeration nozzle (6.1) is connected with an aeration fan (5).
5. The seawater flue gas desulfurization device by the two-stage absorption membrane method according to claim 4, characterized in that: the porous membranes in the first-stage membrane component (2.1) and the second-stage membrane component (2.2) are hydrophilic tubular porous ceramic membranes; wherein the porous membrane has a water drop contact angle of 10 to 50 deg.
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| CN202022812717.XU CN214345523U (en) | 2020-11-27 | 2020-11-27 | Two-stage absorption membrane method seawater flue gas desulfurization device |
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| CN202022812717.XU CN214345523U (en) | 2020-11-27 | 2020-11-27 | Two-stage absorption membrane method seawater flue gas desulfurization device |
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