CN109107368B - Membrane absorption device - Google Patents
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- CN109107368B CN109107368B CN201710495031.2A CN201710495031A CN109107368B CN 109107368 B CN109107368 B CN 109107368B CN 201710495031 A CN201710495031 A CN 201710495031A CN 109107368 B CN109107368 B CN 109107368B
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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- B01D53/78—Liquid phase processes with gas-liquid contact
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Abstract
The invention discloses a film absorption device, comprising: the first membrane contactor is provided with a first gas phase inlet, a first gas phase outlet, a first liquid phase inlet and a first liquid phase outlet; and the second membrane contactor is connected with the first membrane contactor in parallel and is provided with a second gas phase inlet, a second gas phase outlet, a second liquid phase inlet and a second liquid phase outlet. The membrane absorption device has the functions of back washing and back flushing, can effectively control membrane pollution, eliminates the membrane wetting phenomenon generated in the membrane absorption operation process, can continuously produce by alternately operating the first membrane contactor and the second membrane contactor, and does not influence the normal absorption of one membrane contactor in the back washing and back flushing processes of the other membrane contactor, thereby increasing the applicability of the device.
Description
Technical Field
The invention relates to the technical field of oil gas recovery, in particular to a membrane absorption device.
Background
At present, the chemical absorption method is widely applied in the fields of natural gas purification and flue gas treatment, and the method adopts a plate tower or a packed tower, so that the effective mass transfer area is small, the equipment size is large, the engineering construction cost is high, and the problems of entrainment, liquid flooding, liquid leakage and the like are easily caused. And the membrane absorption method of the membrane contact reactor is adopted, gas and absorption liquid respectively flow at two sides of the membrane, so that the operation problems of liquid phase bubbling, entrainment, flooding and the like of a chemical absorption method are avoided, and the volume and the occupied area of the device can be greatly reduced due to the characteristics of large specific surface area, high mass transfer rate and the like of the membrane.
The prior art membrane absorption device mainly uses a membrane contact reactor using a hollow fiber membrane module, but in the membrane separation process, membrane pollution, membrane wetting and the like are inevitably generated along with the progress of absorption reaction. Especially wetting characteristics are one of the important properties of solid surfaces, and in recent years wetting problems have been reduced mainly by using hydrophobic membranes or by performing surface modification of membranes. However, in practical membrane absorption engineering applications, the absorbent solution inevitably penetrates into some of the micropores of the hydrophobic membrane, and even if the membrane is hydrophobic, some wetting may occur due to the nature of the microporous membrane and the operating conditions. If the membrane is wetted, even if the membrane is partially wetted, the mass transfer resistance is also increased remarkably, so that the mass transfer resistance is increased remarkably, the operation efficiency of the device is reduced sharply, and the application of the membrane absorption method is limited greatly.
The prior art is mainly used for solving the problem of membrane pollution, and the problem of membrane wetting is mainly solved by selecting a hydrophobic membrane, so that the problem of membrane wetting caused by long-term operation is not fundamentally solved. The Chinese invention patent CN 102485320A, the device and process for seawater flue gas desulfurization by membrane absorption, adopts hydrophobic hollow fiber membrane, automatic on-line back washing and cleaning process, and on-line cleaning process with multiple nozzles. However, since the hollow fiber membrane modules are bundled, the cleaning effect of the membrane filaments at the central position is not ideal by adopting a nozzle spraying mode, and the problem of membrane wetting can be further aggravated by spraying cleaning liquid. Therefore, a membrane absorption device capable of eliminating a membrane wetting phenomenon generated during a membrane absorption operation is desired.
Disclosure of Invention
The invention aims to provide a membrane absorption device which has the functions of back washing and back blowing, can effectively control membrane pollution and eliminate membrane wetting phenomenon generated in the process of membrane absorption operation.
The invention adopts the following solution:
a film absorbent device comprising:
the first membrane contactor is provided with a first gas phase inlet, a first gas phase outlet, a first liquid phase inlet and a first liquid phase outlet;
the second membrane contactor is connected with the first membrane contactor in parallel and is provided with a second gas phase inlet, a second gas phase outlet, a second liquid phase inlet and a second liquid phase outlet;
the first gas phase inlet and the second gas phase inlet are respectively connected to a raw gas pipeline through a first raw gas pipeline electromagnetic valve and a second raw gas pipeline electromagnetic valve, and are respectively connected to a back-blowing exhaust pipeline through a first back-blowing exhaust pipeline electromagnetic valve and a second back-blowing exhaust pipeline electromagnetic valve;
the first gas phase outlet and the second gas phase outlet are respectively connected to a purifier pipeline through a first purified gas pipeline electromagnetic valve and a second purified gas pipeline electromagnetic valve, and are respectively connected to a back-blowing gas inlet pipeline through a first back-blowing gas inlet pipeline electromagnetic valve and a second back-blowing gas inlet pipeline electromagnetic valve;
the first liquid-phase inlet and the second liquid-phase inlet are respectively connected to the absorbent lean liquid pipeline through a first absorbent lean liquid pipeline electromagnetic valve and a second absorbent lean liquid pipeline electromagnetic valve, and are respectively connected to the backwash water discharge pipeline through a first backwash water discharge pipeline electromagnetic valve and a second backwash water discharge pipeline electromagnetic valve;
the first liquid phase outlet and the second liquid phase outlet are respectively connected to the absorbent rich liquid pipeline through a first absorbent rich liquid pipeline electromagnetic valve and a second absorbent rich liquid pipeline electromagnetic valve, and are respectively connected to the backwashing water inlet pipeline through a first backwashing water inlet pipeline electromagnetic valve and a second backwashing water inlet pipeline electromagnetic valve.
Preferably, the first and second membrane contactors include a housing and a membrane module disposed within the housing.
Preferably, the membrane module is a hollow fiber membrane module.
Preferably, the outer wall of the housing is provided with a plurality of ultrasonic probes.
Preferably, a heater, a thermometer and a temperature transmitter are arranged on the back blowing air inlet pipeline.
Preferably, a first pressure gauge and a first pressure transmitter are arranged on the back blowing air inlet pipeline.
Preferably, a filter is arranged on the back-blowing air inlet pipeline.
Preferably, a water dew point analyzer and a water dew point transmitter are arranged on the back blowing exhaust pipeline.
Preferably, a suspended matter detector and a suspended matter transmitter are arranged on the back flushing drainage pipeline.
Preferably, a second pressure gauge and a second pressure transmitter are provided on the absorbent lean liquid line.
Compared with the prior art, the invention has the beneficial effects that:
firstly, the membrane has the functions of back washing and back flushing, can effectively control membrane pollution, and eliminates the membrane wetting phenomenon generated in the membrane absorption operation process, thereby reducing mass transfer resistance, improving the absorption effect of membrane absorption, and maintaining good mass transfer performance in the long-term operation process;
secondly, the first membrane contactor and the second membrane contactor alternately operate, continuous production can be realized, and the normal absorption of one membrane contactor is not influenced in the back washing and back blowing processes of the other membrane contactor, so that the applicability of the device is improved;
thirdly, a plurality of ultrasonic probes are arranged on the outer wall of the membrane contactor, and ultrasonic waves are transmitted to the surface of the membrane component by utilizing the characteristic that liquid can effectively transmit the ultrasonic waves, so that the backwashing effect on the membrane component can be effectively enhanced, and the backwashing time is shortened;
fourthly, controlling the back flushing time through a water dew point analyzer, and reducing the back flushing consumption;
fifthly, the backwashing time is controlled by a suspended matter detector, so that ineffective backwashing is avoided.
The method and apparatus of the present invention have other features and advantages which will be apparent from or are set forth in detail in the accompanying drawings and the following detailed description, which are incorporated herein, and which together serve to explain certain principles of the invention.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
FIG. 1 shows a schematic view of a membrane absorption device according to an embodiment of the invention;
fig. 2 shows a schematic view of a membrane contactor of a membrane absorption device according to an embodiment of the present invention.
Description of reference numerals:
1 a-a first membrane contactor, 1 b-a second membrane contactor;
21 a-a first gas phase inlet, 21 b-a second gas phase inlet;
22 a-a first gas phase outlet, 22 b-a second gas phase outlet;
31 a-a first liquid phase inlet, 31 b-a second liquid phase inlet;
32 a-a first liquid phase outlet, 32 b-a second liquid phase outlet;
2-a heater, 3-a filter, 4-a thermometer, 5-a temperature transmitter, 6-a first pressure gauge, 7-a first pressure transmitter, 8-a water dew point analyzer, 9-a second pressure gauge, 10-a second pressure transmitter, 11-an ultrasonic probe, 12-a shell, 13-a membrane component, 14-a water dew point transmitter, 15-a suspended matter detector, 16-a suspended matter transmitter;
101 a-first feed gas line solenoid valve, 101 b-second feed gas line solenoid valve;
102 a-a first purge gas line solenoid valve, 102 b-a second purge gas line solenoid valve;
103 a-first absorbent lean liquid line solenoid valve, 103 b-second absorbent lean liquid line solenoid valve;
104 a-a first absorbent rich liquid line solenoid valve, 104 b-a second absorbent rich liquid line solenoid valve;
105 a-a first backwash water inlet pipeline electromagnetic valve, 105 b-a second backwash water inlet pipeline electromagnetic valve;
106 a-a first backwash drain line solenoid valve, 106 b-a second backwash drain line solenoid valve;
107 a-a first back-blowing air inlet pipeline electromagnetic valve, and 107 b-a second back-blowing air inlet pipeline electromagnetic valve;
108 a-a first back-blowing exhaust line solenoid valve, and 108 b-a second back-blowing exhaust line solenoid valve.
Detailed Description
The invention will be described in more detail below with reference to the accompanying drawings. While the preferred embodiments of the present invention are shown in the drawings, it should be understood that the present invention may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
Fig. 1 shows a schematic view of a membrane absorption device according to an embodiment of the present invention, and fig. 2 shows a schematic view of a membrane contactor of the membrane absorption device according to an embodiment of the present invention.
As shown in fig. 1, a film absorbing apparatus according to an embodiment of the present invention includes:
a first membrane contactor 1a, the first membrane contactor 1a being provided with a first gas phase inlet 21a, a first gas phase outlet 22a, a first liquid phase inlet 31a, a first liquid phase outlet 32 a;
a second membrane contactor 1b, the second membrane contactor 1b being arranged in parallel with the first membrane contactor 1a, the second membrane contactor 1b being provided with a second gas phase inlet 21b, a second gas phase outlet 22b, a second liquid phase inlet 31b, a second liquid phase outlet 32 b;
the first gas phase inlet 21a and the second gas phase inlet 21b are respectively connected to a raw gas pipeline through a first raw gas pipeline electromagnetic valve 101a and a second raw gas pipeline electromagnetic valve 101b, and are respectively connected to a back-blowing exhaust pipeline through a first back-blowing exhaust pipeline electromagnetic valve 108a and a second back-blowing exhaust pipeline electromagnetic valve 108 b;
the first gas phase outlet 22a and the second gas phase outlet 22b are respectively connected to the purifier pipeline through a first purified gas pipeline electromagnetic valve 102a and a second purified gas pipeline electromagnetic valve 102b, and are respectively connected to the back-blowing gas inlet pipeline through a first back-blowing gas inlet pipeline electromagnetic valve 107a and a second back-blowing gas inlet pipeline electromagnetic valve 107 b;
the first liquid-phase inlet 31a and the second liquid-phase inlet 31b are connected to the absorbent lean liquid line through a first absorbent lean liquid line solenoid valve 103a and a second absorbent lean liquid line solenoid valve 103b, respectively, and are connected to the backwash drain line through a first backwash drain line solenoid valve 106a and a second backwash drain line solenoid valve 106b, respectively;
the first liquid-phase outlet 32a and the second liquid-phase outlet 32b are connected to the absorbent rich liquid line through a first absorbent rich liquid line solenoid valve 104a and a second absorbent rich liquid line solenoid valve 104b, respectively, and are connected to the backwash water inlet line through a first backwash water inlet line solenoid valve 105a and a second backwash water inlet line solenoid valve 105b, respectively.
The first membrane contactor 1a and the second membrane contactor 1b alternately operate, only one membrane contactor is started during normal absorption, and the other membrane contactor is reserved. When the purified gas output by the gas component analyzer is unqualified, the membrane contactor for absorption is switched to a back washing mode and a back flushing mode, and the standby membrane contactor is started for gas purification.
The operation of the membrane absorption device according to the embodiment of the present invention is described in detail below with reference to fig. 1. When the first membrane contactor 1a is opened, the first raw material gas line solenoid valve 101a, the first purified gas line solenoid valve 102a, the first absorbent lean liquid line solenoid valve 103a, and the first absorbent rich liquid line solenoid valve 104a are opened, and the first backwash water inlet line solenoid valve 105a, the first backwash water discharge line solenoid valve 106a, the first back-flushing gas inlet line solenoid valve 107a, and the first back-flushing gas outlet line solenoid valve 108a are closed. The second membrane contactor 1b is ready for use, and all the electromagnetic valves connected to the second membrane contactor 1b are closed.
A gas to be purified (i.e., a raw material gas) a1 enters a shell side of the first membrane contactor 1a through a first gas phase inlet 21a, an absorbent lean solution B1 enters a tube side of the first membrane contactor 1a through a first liquid phase inlet 31a, a component to be purified in the gas to be purified a1 reacts with the absorbent lean solution B1 in the first membrane contactor 1a to be absorbed, the purified gas a2 is discharged from a first gas phase outlet 22a of the first membrane contactor 1a, and at the same time, an absorbed absorbent rich solution B2 is discharged through a first liquid phase outlet 32 a.
When the absorption effect of the first membrane contactor 1a is not ideal and backwashing and back flushing are required, the first raw material gas pipeline electromagnetic valve 101a, the first purified gas pipeline electromagnetic valve 102a, the first absorbent lean liquid pipeline electromagnetic valve 103a, the first absorbent rich liquid pipeline electromagnetic valve 104a, the first back flushing gas inlet pipeline electromagnetic valve 107a and the first back flushing gas exhaust pipeline electromagnetic valve 108a are closed, the first back flushing water inlet pipeline electromagnetic valve 105a and the first back flushing water exhaust pipeline electromagnetic valve 106a are opened, and back flushing liquid is firstly adopted for back flushing. Backwash liquid C1 enters through the first liquid phase outlet 32a of the first membrane contactor 1a and used backwash liquid C2 is discharged from the first liquid phase inlet 31 a. After the backwashing is finished, the first backwashing water inlet pipeline electromagnetic valve 105a and the first backwashing water discharge pipeline electromagnetic valve 106a are closed, the first back-blowing air inlet pipeline electromagnetic valve 107a and the first back-blowing air discharge pipeline electromagnetic valve 108a are opened, and the first membrane contactor 1a is subjected to back-blowing and drying. The blowback gas D1 enters through the first gas phase outlet 22a of the first membrane contactor 1a, and the used blowback gas D2 is discharged through the first gas phase inlet 21 a. And closing all the electromagnetic valves connected with the first membrane contactor 1a after the back flushing is finished, and keeping the first membrane contactor 1a for later use. In fig. 1, the arrows indicate the flow direction of the fluid.
And starting the second membrane contactor 1b for absorption while the first membrane contactor 1a performs backwashing and back flushing. The second membrane contactor 1b operates similarly to the first membrane contactor 1 a: during absorption, the second raw material gas pipeline electromagnetic valve 101b, the second purified gas pipeline electromagnetic valve 102b, the second absorbent lean liquid pipeline electromagnetic valve 103b and the second absorbent rich liquid pipeline electromagnetic valve 104b are opened, and the second backwashing water inlet pipeline electromagnetic valve 105b, the second backwashing water discharge pipeline electromagnetic valve 106b, the second backwashing gas inlet pipeline electromagnetic valve 107b and the second backwashing gas discharge pipeline electromagnetic valve 108b are closed.
The gas to be purified (i.e., the raw gas) a1 enters the shell side of the second membrane contactor 1B through the second gas phase inlet 21B, the absorbent lean solution B1 enters the tube side of the second membrane contactor 1B through the second liquid phase inlet 31B, the component to be purified in the gas to be purified a1 reacts with the absorbent lean solution B1 in the second membrane contactor 1B to be absorbed, the purified gas a2 is discharged from the second gas phase outlet 22B of the second membrane contactor 1B, and at the same time, the absorbed absorbent rich solution B2 is discharged through the second liquid phase outlet 32B.
When the absorption effect of the second membrane contactor 1b is not ideal and back flushing are needed, the first membrane contactor 1a is started to absorb, and the second membrane contactor 1b is subjected to back flushing and back flushing. The backwashing and back-flushing processes of the second membrane contactor 1b are similar to those of the first membrane contactor 1a, and are not described in detail herein.
The membrane absorption device provided by the embodiment of the invention has the functions of back flushing and back flushing, can effectively control membrane pollution, and eliminates the membrane wetting phenomenon generated in the membrane absorption operation process, thereby reducing mass transfer resistance, improving the absorption effect of membrane absorption, and maintaining good mass transfer performance in the long-term operation process. In addition, the first membrane contactor and the second membrane contactor alternately operate, continuous production can be realized, and the normal absorption of the other membrane contactor is not influenced in the back washing and back blowing processes of one membrane contactor, so that the applicability of the device is improved.
In one example, the first membrane contactor 1a and the second membrane contactor 1b are identical in structure, and each includes a housing 12 and a membrane module 13 disposed within the housing, as shown in fig. 2. Preferably, the membrane module 13 is a hollow fiber membrane module, and the gas to be purified and the absorbent barren solution form a reaction interface at the micropores of the hollow fiber membrane module, and the gas is absorbed. The membrane component can be selected from polypropylene (PP), Polytetrafluoroethylene (PTFE), polyvinylidene fluoride (PVDF) and other materials, or the materials are subjected to hydrophobicity improvement treatment, or a composite membrane material is directly adopted.
In one example, a plurality of ultrasonic probes 11 are provided on an outer wall of the housing 12, as shown in fig. 2. In the back washing process, the ultrasonic probe is started, and ultrasonic waves are transmitted to the surface of the membrane component by utilizing the characteristic that liquid can effectively transmit the ultrasonic waves, so that the back washing effect on the membrane component can be effectively enhanced, and the back washing time is shortened. The ultrasonic probes 11 may be uniformly distributed on the outer wall of the housing 12.
In one example, a heater 2, a thermometer 4 and a temperature transmitter 5 are provided on the blowback intake line. The heating is carried out through the heater 2, and the back blowing temperature is obtained through the thermometer 4 and the temperature transmitter 5, so that the back blowing temperature can be controlled, the back blowing effect is improved, and the condition that the back blowing temperature is not too high so as to cause irreversible damage to the membrane is ensured. The blow-back temperature generally does not exceed 80 ℃.
In one example, a first pressure gauge 6 and a first pressure transmitter 7 are provided on the blowback air intake line to detect blowback air pressure.
In one example, the back-blowing air inlet pipeline is provided with a filter 3, and the filter 3 can filter back-blowing air to prevent solid particles possibly carried in the back-blowing air from damaging the membrane material.
In one example, the backwash water discharge line is provided with a suspended matter detector 15 and a suspended matter transmitter 16, and the backwash time is determined according to the suspended matter content measured by the suspended matter detector. And (4) gradually reducing the content of the solid suspended matters and stabilizing the content of the solid suspended matters along with the back flushing, and stopping the back flushing after the content of the solid suspended matters is stabilized.
In one example, a water dew point analyzer 8 and a water dew point transmitter 14 are provided on the blowback exhaust line, and the blowback time is determined based on the water dew point measured by the water dew point analyzer. And (4) gradually reducing the water dew point along with the back flushing, and stopping the back flushing when the water dew point reaches a set value. The water dew point is generally set at 0 ℃.
In one example, a second pressure gauge 9 and a second pressure transmitter 10 are provided on the absorbent lean liquid line to detect the pressure of the absorbent lean liquid.
The membrane absorption device according to the present invention is described below with reference to two membrane contactors, and it can be understood by those skilled in the art that more than two membrane contactors may be arranged in parallel in the membrane absorption device according to actual needs, so as to realize simultaneous absorption of a plurality of membrane contactors and simultaneous standby of another plurality of membrane contactors.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments. The terminology used herein was chosen in order to best explain the principles of the embodiments, the practical application, or improvements made to the technology in the marketplace, or to enable others of ordinary skill in the art to understand the embodiments disclosed herein.
Claims (10)
1. A film absorbent device comprising:
a first membrane contactor (1a), the first membrane contactor (1a) being provided with a first gas phase inlet (21a), a first gas phase outlet (22a), a first liquid phase inlet (31a), a first liquid phase outlet (32 a);
a second membrane contactor (1b), the second membrane contactor (1b) being arranged in parallel with the first membrane contactor (1a), the second membrane contactor (1b) being provided with a second gas phase inlet (21b), a second gas phase outlet (22b), a second liquid phase inlet (31b), a second liquid phase outlet (32 b);
the system is characterized in that the first gas phase inlet (21a) and the second gas phase inlet (21b) are respectively connected to a raw gas pipeline through a first raw gas pipeline electromagnetic valve (101a) and a second raw gas pipeline electromagnetic valve (101b), and are respectively connected to a back-blowing exhaust pipeline through a first back-blowing exhaust pipeline electromagnetic valve (108a) and a second back-blowing exhaust pipeline electromagnetic valve (108 b);
the first gas phase outlet (22a) and the second gas phase outlet (22b) are respectively connected to a purifier pipeline through a first purified gas pipeline electromagnetic valve (102a) and a second purified gas pipeline electromagnetic valve (102b), and are respectively connected to a back-blowing gas inlet pipeline through a first back-blowing gas inlet pipeline electromagnetic valve (107a) and a second back-blowing gas inlet pipeline electromagnetic valve (107 b);
the first liquid-phase inlet (31a) and the second liquid-phase inlet (31b) are connected to the absorbent lean line through a first absorbent lean line solenoid valve (103a) and a second absorbent lean line solenoid valve (103b), respectively, and are connected to the backwash drain line through a first backwash drain line solenoid valve (106a) and a second backwash drain line solenoid valve (106b), respectively;
the first liquid phase outlet (32a) and the second liquid phase outlet (32b) are connected to the absorbent rich liquid line through a first absorbent rich liquid line solenoid valve (104a) and a second absorbent rich liquid line solenoid valve (104b), respectively, and are connected to the backwash water inlet line through a first backwash water inlet line solenoid valve (105a) and a second backwash water inlet line solenoid valve (105b), respectively.
2. The membrane absorption device according to claim 1, wherein the first and second membrane contactors (1a, 1b) comprise a housing (12) and a membrane module (13) disposed within the housing (12).
3. A membrane absorption unit according to claim 2, wherein the membrane module (13) is a hollow fiber membrane module.
4. The membrane absorption device according to claim 2, wherein a plurality of ultrasonic probes (11) are provided on an outer wall of the housing (12).
5. The film absorber as claimed in claim 1, wherein the blowback air inlet line is provided with a heater (2), a thermometer (4) and a temperature transmitter (5).
6. The membrane absorber according to claim 1, wherein a first pressure gauge (6) and a first pressure transmitter (7) are provided on the blowback air inlet line.
7. The membrane absorption device according to claim 1, wherein a filter (3) is arranged on the blowback air inlet line.
8. Membrane absorption device according to claim 1, wherein a water dew point analyzer (8) and a water dew point transmitter (14) are provided on the blow-back exhaust line.
9. The membrane absorption device according to claim 1, wherein a suspension detector (15) and a suspension transmitter (16) are provided on the backwash drain line.
10. The membrane absorber according to claim 1, wherein a second pressure gauge (9) and a second pressure transmitter (10) are provided on the absorber lean liquid line.
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| CN201710495031.2A CN109107368B (en) | 2017-06-26 | 2017-06-26 | Membrane absorption device |
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| CN201710495031.2A CN109107368B (en) | 2017-06-26 | 2017-06-26 | Membrane absorption device |
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| CN109107368B true CN109107368B (en) | 2021-05-25 |
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| CN114073992A (en) * | 2020-08-14 | 2022-02-22 | 中国石油化工股份有限公司 | Oxygen-enriched regeneration device and method for redox desulfurization process and application |
| CN115253598B (en) * | 2022-07-12 | 2023-04-28 | 青岛海湾化工设计研究院有限公司 | For CO 2 Trapped tower absorption membrane contactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IL39983A0 (en) * | 1971-09-10 | 1972-09-28 | Wright H D | Method and apparatus for removing pollutants from air or similar gases |
| DE19639965A1 (en) * | 1996-09-27 | 1998-04-02 | Gore W L & Ass Gmbh | Separation of components of a gas mixture through membranes |
| CN2369748Y (en) * | 1999-04-26 | 2000-03-22 | 浙江大学膜分离工程联合公司 | Film type mixed gas component remover |
| CN1488422A (en) * | 2003-07-30 | 2004-04-14 | 浙江大学 | Method and system for separating carbon dioxide form fume by hollow film membrane contactor |
| CN102485320B (en) * | 2010-12-05 | 2013-09-18 | 国家海洋局天津海水淡化与综合利用研究所 | Device for desulfurizing flue gas by seawater through membrane absorption and its process |
| CN203355566U (en) * | 2012-09-24 | 2013-12-25 | 张志� | System for recycling carbon dioxide from boiler flue gas |
| CN103331095B (en) * | 2013-07-16 | 2015-01-14 | 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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