CN107952330A - A kind of smoke eliminator and technique - Google Patents
A kind of smoke eliminator and technique Download PDFInfo
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- CN107952330A CN107952330A CN201711250248.3A CN201711250248A CN107952330A CN 107952330 A CN107952330 A CN 107952330A CN 201711250248 A CN201711250248 A CN 201711250248A CN 107952330 A CN107952330 A CN 107952330A
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/60—Combinations of devices covered by groups B01D46/00 and B01D47/00
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D46/54—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms
- B01D46/543—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms using membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2257/10—Single element gases other than halogens
- B01D2257/104—Oxygen
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D2258/00—Sources of waste gases
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
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Abstract
The present invention provides the purifier and technique of a kind of flue gas, it is by the way that seawater desalination system and seawater electrolysis system are coupled, the desulphurization denitration decarburization of flue gas is realized by the HClO liquid streams of electrolytic seawater preparation strong oxidizing property and the NaOH liquid streams of alkalescence and by the alkalescence of seawater itself, resource utilization is high, and gas cleaning effect is good.
Description
Technical field
This application involves the environment friendly purification apparatus and technique of a kind of flue gas, and in particular to a kind of desulphurization denitration decarburization of flue gas
Device and technique.
Background technology
At present, industrial boilers in China field is all that high energy consumption is poorly efficient, conventional chain boiler of maximum discharge, the heat of boiler
Efficiency is generally all between 60-65%.Wherein, coal-burning boiler can discharge substantial amounts of SO2, nitrogen oxides (NOx) and CO2Gas etc.,
SO2, NOx be the main component of atmosphere pollution, and form the main matter of acid rain and photochemical fog, and CO2Isothermal chamber gas
The environmental problems such as caused greenhouse effects, have not only broken up the ecosystem but also have compromised health.These environmental problems
The economic society risk and heavy losses brought, have undoubtedly become relation China sustainable economic development even social harmony and have stablized
Significant problem.
In the prior art, to SO2Control, more mature technology is limestone-gypsum method at present, its main feature is that system
Stable, removal efficiency is up to more than 95%.And for the control of NOx, frequently with selective catalytic reduction (SCR), take off
Except efficiency is up to more than 90%, but there is investment and operating cost height, the difficult life of catalyst easy in inactivation, may cause secondary dirt in it
The problems such as dye.Country's coal-burning boiler desulphurization denitration is generally using the combination technique of FGD and SCR at present, but the technology is answered
Miscellaneous, investment and operating cost are high.And decarburization is then generally using improvement hot potash method abjection CO2, its main feature is that it is efficient, but need
Want a large amount of lye.
In recent years, it is more and more as the technology of desulphurization denitration absorbing liquid using seawater, compared to traditional lime-stone
Cream method is compared, and sea water desulfuration cost is low, therefore is having great application potential by sea region.However, in the prior art using sea
Water is only limitted to desulfurization and/or denitration, and there has been no a kind of technology can realize desulphurization denitration decarburization, and there is an urgent need for the application technology to seawater
Improved.
The content of the invention
To solve the above problems, purifier and technique the present invention provides a kind of flue gas.
The present invention provides a kind of flue gas desulfurization and denitrification decarbonation appliance of resourcebility, it can be efficiently removed in flue gas
SO2、NOX、CO2Deng pollutant and carry out recycling.
The present invention is as follows using technical solution：
A kind of purifier of flue gas, it includes seawater treatment system and smoke processing system；Seawater treatment system is included successively
Filter, RO films, mud chamber and the tank house of connection；Smoke processing system include sequentially connected spray chamber A,
Membrane contactor, spray chamber B, drier；Wherein, two outlets of spray chamber A, the absorbing liquid entrance of spray chamber B and tank house connect
Connect, the liquid phase entrance of membrane contactor is connected with filter outlet, membrane contactor, the liquid-phase outlet of spray chamber B and RO films it is dense
Contracting seawer outlet is connected with the liquid phase entrance of mud chamber, and the gas vent of spray chamber B is connected with drier, chimney successively.
Preferably, the tank house is diaphragm electrolysis apparatus, its by seawater electrolysis for strong oxidizing property HClO liquid streams and
The NaOH liquid streams of alkalescence, wherein HClO fluid outlets are connected with spray chamber A, and NaOH fluid outlets are connected with spray chamber B.
Preferably, storage tank A is set between RO films and mud chamber, storage tank B, electrolysis are set between tank house and spray chamber A
Storage tank C is set between room and spray chamber B, storage tank D, the liquid-phase outlet of spray chamber B and storage are set between membrane contactor and mud chamber
Tank D connections.
Preferably, centrifugal pump is set between filter and RO films.
Preferably, heat exchanger and deduster are also disposed with before gas mixer.
Preferably, spray chamber liquid-phase outlet connection mixing chamber liquid phase entrance, another liquid-phase outlet of mixing chamber with
Ammonium hydroxide connects, and the liquid-phase outlet of mixing chamber is connected with crystallisation chamber.
Preferably, the outlet of spray chamber B is also connected with hothouse, hothouse and O2Selective absorption device connects, O2Selectivity
Filling O in absorber2Selective absorbent, O2Mixed with being arranged on the gas before spray chamber A the desorption gas outlet of selective absorption device
Clutch connects.Preferably, O2Selective absorbent is carbon molecular sieve.
Preferably, membrane contactor is hollow fiber membrane contactors, and wherein gas is into tube side, and liquid is into shell side, doughnut
The material of film is the one or more in Kynoar, polytetrafluoroethylene (PTFE), polypropylene, polyethylene or polysulfones, and contact angle is more than
110 °, porosity is more than 50-60%, and aperture is 0.2-1 μm.
Preferably, gas mixer is static mixer, it is preferable that static mixer is single-screw static mixer or double
Helical static mixer.
Present invention also offers a kind of purification technique of flue gas, it includes comprising the following steps：
A kind of flue gas purifying technique, it is characterised in that comprise the following steps：
（1）Fresh seawater is subjected to filtering and impurity removing by filter, and is passed through after centrifugal pump pressurizes in RO films and realizes sea water desalination,
Wherein penetrating fluid clear water is passed through in mud chamber as output of products, seepage remaining liquid concentrated seawater through storage tank A, with from membrane contactor,
Liquid mixed precipitation in spray chamber B, will the outer row of solid precipitation, supernatant liquid be passed through in tank house electrolysis for HClO liquid streams and
NaOH liquid streams, wherein, HClO liquid streams are passed through at the top of spray chamber A through storage tank B, and NaOH liquid streams are passed through at the top of spray chamber B through storage tank C；
（2）Flue gas enters in spray chamber A after heat exchanger heat exchange and deduster carry out dedusting from spray chamber A bottoms successively, with
HClO liquid streams from tank house inversely contact the desulphurization denitration for realizing gas, and liquid product enters in mixing chamber, mixed with ammonium hydroxide
Close, adjust pH value, obtain the mixed liquor containing ammonium nitrate, ammonium sulfate and ammonium chloride；
（3）By step（2）Obtained mixed liquor obtains ammonium sulfate, ammonium nitrate and chlorination by being evaporated crystallization in crystallisation chamber
The crude product output of ammonium；
（4）Gas at the top of from spray chamber A out enters the tube side of membrane contactor, and the shell side of membrane contactor is passed through by filter mistake
Absorption occurs for the seawater of filter, the membrane component surface inside membrane contactor to realize the preliminary decarburization of gas；
（5）By step（4）Gas continue through the bottom of spray chamber B and be passed through in spray chamber B, with the NaOH liquid from tank house
The gross decarburization of gas is realized in the reverse contact of stream, and is emptied after decarburization after drier desiccant dehumidification by chimney, and film is connect
It is passed through after the liquid mixing of liquid and spray chamber the B discharge of the discharge of tentaculum in mud chamber.
Preferably, the technique is in step（5）Also there is step afterwards（6）Gas after desiccant dehumidification is delivered to O2Selectivity
To the O in gas in absorber2Selective absorption, gas not to be adsorbed are passed through chimney emptying, O2 are selected after adsorption saturation
Property absorber carry out regeneration desorption, the gas after desorption is delivered in gas buffer tank, and continue to be passed through be arranged on spray chamber A and
Mixed in gas mixer between deduster with flue gas.
Technical scheme principle is as follows：
（1）Water removal, NaCl are outside also containing suspended matter, K in seawater+、Mg2+、Ca2+Deng wherein suspended matter, Mg2+、Ca2+After influencing
Continuous electrolysis process and decarbonization process, it is therefore desirable to which, by filter to remove suspended matter, preferable filter filtering accuracy is
0.2-5μm.NaCl contents are not high in seawater, and Direct Electrolysis causes inefficiency, it is necessary to concentration be carried out to seawater, using RO
Film（Reverse osmosis membrane）Directly electrolyzable concentrated seawater and the clear water without salinity can be separated into by seawater, clear water can conduct
Output of products.
（2）Concentrated seawater is electrolysed, uses the mode of diaphragm electrolysis can be by seawater electrolysis for strong oxidizing property
The NaOH liquid streams of HClO liquid streams and strong basicity, wherein HClO can be used for desulphurization denitration, and specific reaction is as follows：
HClO+SO2+H2O→H2SO4+HCl；
HClO+NO → NO2+HCl。
But NO2Easily generation NO, i.e. NO is reacted with water2+H2O→HNO3+ NO, therefore can select to be passed through by gas
By gas and O before in spray chamber A2Mixing（Static mixer, such as single-screw or twin-spiral mixer can be used）, occur
React NO2+H2O+O2→HNO3, so as to avoid NO to a certain extent2NO is reduced to again.Liquid product after gas-liquid contact
Including H2SO4、HCl、HNO3, this programme, which mixes the liquid phase mixture with ammonium hydroxide, occurs acid-base neutralization reaction, sequentially generates as sulphur
Sour ammonium, ammonium chloride and ammonium nitrate, by adjusting its concentration and crystallization temperature, it is possible to achieve the crude separation of above-mentioned three kinds of materials, can
To select three kinds of crude products as output of products can also to be refined to crude product by recrystallization technology.
（3）In the tube side that membrane contactor will be passed through by the gas of desulphurization denitration, connect film is passed through by the seawater of filtering
In the shell side of tentaculum, the fluid isolation of two kinds of phases is opened by membrane component, the CO in gas2Seawater is diffused into by fenestra
In, absorbing reaction occurs on the surface of membrane component, realizes preliminary decarbonizing process, naturally it is also possible to which selection is by by the concentration of RO films
Seawater, which is passed through in membrane contactor, carries out preliminary carbonization treatment, its reaction is CO2+H2O→H2CO3, CO3 2--+CO2+H2O→HCO3-。
Due to the process decarburization and it is not thorough, it is necessary to the further carbonization treatment of gas.The NaOH that this programme is produced being electrolysed is as spray
The absorbing liquid of room B is drenched, CO3 is generated after gas liquid reaction2-, itself and have neither part nor lot in the HCO that the OH- of reaction is further contacted with from film3-
Mixed in storage tank D, wherein OH-+HCO3 2-→CO3 2-+H2O, CO therein3 2-In mud chamber with the Ca in concentrated seawater2+、
Mg2+Ionic reaction makes its precipitation, avoids influencing follow-up electrolytic process.
（4）Contain a certain amount of NOx, H in flue gas after desulphurization denitration decarburization2O、N2、O2, flue gas at this time accorded with
Atmospheric emission standard is closed, can be selected its outer row.It is of course also possible to select to be utilized, such as it is further done
Nitrogen selective absorber is passed through after dry to N2Making choice property is adsorbed, it is not to be adsorbed wherein in contain NOXAnd O2Can with it is first
Beginning flue gas mixes, and on the one hand can further reduce NO in flue gasXContent, is on the other hand supplied to the enough oxygen contents of flue gas.
But due to the N in market2Adsorbent（Such as clinoptilolite）To N2Adsorptive selectivity it is not high, therefore can select will be dry
Flue gas after dry is passed through O2Selective absorption device adsorbs making choice property of oxygen, gas not to be adsorbed emptying, full to adsorbing
The adsorbent of sum carries out regeneration desorption, and desorption gas is mixed with raw flue gas.Since whole technique is continuous, preferably use
Multiple equivalent O2The parallel connection of selective absorption device is to realize absorption/regenerative process of absorber.Absorber can select PSA to adsorb
Device, can also selected as TSA absorbers.Certainly, oxygen concentration is different in different flue gases, can when oxygen content is low in flue gas
To select the inlet porting in gas buffer tank that to be passed through the oxygen in the external world, the 3rd can also be set on gas mixer
Gas access is passed through extraneous oxygen, and extraneous oxygen can select the oxygen that electrolysis is obtained by the water purification of RO membrane filtrations.
Relative to the prior art, the present invention has the following advantages：
1. whole system of the present invention realize using seawater as raw material carry out flue gas desulphurization denitration decarbonizing process, product have clear water and
May be used as the ammonium salt of fertilizer, be effectively utilized seawater alkalescence and flue gas in sour gas, good economy performance.
2. the present invention obtains the HClO and overbasic NaOH of high oxidative by electrolytic seawater, need not add substantially
Other absorbents can complete fume treatment process, and gas cleaning effect is good.
3. the present invention can realize particulate matter in flue gas, SO2、NOX、CO2、H2The high-efficient purification of the pollutants such as O, using this
Technology can realize SO2Removal efficiency is more than 98.5%, NO and NOXRemoval efficiency be more than 70%, CO2Removal efficiency be more than 99%.
Brief description of the drawings
The present invention is further described in conjunction with the accompanying drawings and embodiments：
Attached drawing 1 is the schematic diagram of the embodiment 1 of the flue gas desulfurization and denitrification decarbonization device of the present invention.
Attached drawing 2 is the schematic diagram of the embodiment 2 of the flue gas desulfurization and denitrification decarbonization device of the present invention.
Embodiment
It is further details of explanation to the present invention presently in connection with drawings and examples.The attached drawing is simplified schematic diagram,
Only illustrate the essential structure of the present invention in a schematic way, therefore it only shows composition related to the present invention.
Embodiment 1
A kind of purifier of flue gas, it includes seawater treatment system and smoke processing system；Seawater treatment system is included successively
Filter, centrifugal pump, RO films, storage tank A, storage tank B, storage tank C, mud chamber and the diaphragm electrolysis room of connection；Smoke processing system bag
Include sequentially connected heat exchanger, deduster, spray chamber A, membrane contactor, spray chamber B, drier, chimney.Its
In, the outlet of filter is divided into two branches, and one is connected with centrifugal pump, and another is connected with membrane contactor, with respectively by newly
To membrane contactor desulfurization and RO film sea water desalinations, RO films are connected with the seawater that will be concentrated by RO films fresh sea water supply with storage tank A
It is stored in storage tank A, storage tank A is connected with mud chamber to realize Mg2+、Ca2+Precipitation, the seawater after precipitation enters diaphragm electrolysis
Room by seawater electrolysis for strong oxidizing property HClO liquid streams and strong basicity NaOH liquid streams, wherein, HClO liquid streams are stored in storage tank B
And be further connected with spray chamber A to realize desulphurization denitration, NaOH liquid streams are connected with storage tank C and are further connected with spray chamber B
To realize thorough decarburization, the liquid-phase outlet of spray chamber A is connected with mixing chamber, and another entrance input ammonium hydroxide of mixing chamber, liquid phase is mixed
Compound and ammonium hydroxide hybrid reaction generation ammonium salt, the liquid-phase outlet of mixing chamber is connected with crystallisation chamber realizes the coarse crystallization of ammonium salt.Spray
The gas phase entrance of room A is connected with deduster and heat exchanger successively.The gas vent of spray chamber A is connected with membrane contactor to realize
Using the purpose of the preliminary decarburization of fresh seawater, the gaseous phase outlet of membrane contactor is connected with spray chamber B by flue gas and to come from membrane
Thorough decarburization, the liquid-phase outlet of membrane contactor and the liquid phase of spray chamber B are realized in the reverse contact in it of the NaOH lye of tank house
Outlet is connected with storage tank D, and storage tank D is further connected with mud chamber.The gaseous phase outlet of spray chamber B successively with drier, chimney
Connection is emptied with will purify the flue gas after dehumidifying.
The operating procedure of above device comprises the following steps：
（1）Fresh seawater is subjected to filtering and impurity removing by filter, and is passed through after centrifugal pump pressurizes in RO films and realizes sea water desalination,
Wherein penetrating fluid clear water is passed through in mud chamber as output of products, seepage remaining liquid concentrated seawater through storage tank A, with from membrane contactor,
Liquid mixed precipitation in spray chamber B, will the outer row of solid precipitation, supernatant liquid be passed through in tank house electrolysis for HClO liquid streams and
NaOH liquid streams, wherein, HClO liquid streams are passed through at the top of spray chamber A through storage tank B, and NaOH liquid streams are passed through at the top of spray chamber B through storage tank C；
（2）Flue gas enters in spray chamber A after heat exchanger heat exchange and deduster carry out dedusting from spray chamber A bottoms successively, with
HClO liquid streams from tank house inversely contact the desulphurization denitration for realizing gas, and liquid product enters in mixing chamber, mixed with ammonium hydroxide
Close, adjust pH value, obtain the mixed liquor containing ammonium nitrate, ammonium sulfate and ammonium chloride；
（3）By step（2）Obtained mixed liquor obtains ammonium sulfate, ammonium nitrate and chlorination by being evaporated crystallization in crystallisation chamber
The crude product output of ammonium；
（4）Gas at the top of from spray chamber A out enters the tube side of membrane contactor, and the shell side of membrane contactor is passed through by filter mistake
Absorption occurs for the seawater of filter, the membrane component surface inside membrane contactor to realize the preliminary decarburization of gas；
（5）By step（4）Gas continue through the bottom of spray chamber B and be passed through in spray chamber B, with the NaOH liquid from tank house
The gross decarburization of gas is realized in the reverse contact of stream, and is emptied after decarburization after drier is dried by chimney, by membrane contactor
Discharge liquid and spray chamber B discharge liquid mixing after be passed through in mud chamber.
Using the specific effect of this technique referring to table 1
| SO2（ppm） | NOX（ppm） | CO2（V%） | |
| Before processing | 2400 | 2000 | 12 |
| After processing | 24 | 550 | 0.084 |
| Conversion ratio | 90.0% | 72.5% | 99.3% |
Embodiment 2
A kind of smoke eliminator, it includes seawater treatment system and smoke processing system；Seawater treatment system includes connecting successively
Filter, centrifugal pump, RO films, storage tank A, storage tank B, storage tank C, mud chamber and the diaphragm electrolysis room connect；Smoke processing system includes
Sequentially connected heat exchanger, deduster, gas mixer, spray chamber A, membrane contactor, spray chamber B, chimney,
Drier, O2Selective absorption device, gas buffer tank.Wherein, the outlet of filter is divided into two branches, one with centrifugal pump phase
Even, another is connected with membrane contactor, fresh seawater is supplied to membrane contactor desulfurization and RO film sea water desalinations, RO films respectively
It is connected with storage tank A will be stored in by the seawater of RO films concentration in storage tank A, storage tank A is connected with mud chamber to realize Mg2+、Ca2 +Precipitation, seawater after precipitation enters HClO liquid stream and strong basicity of the diaphragm electrolysis room by seawater electrolysis for strong oxidizing property
NaOH liquid streams, wherein, HClO liquid streams are stored in storage tank B and are further connected with spray chamber A to realize desulphurization denitration, NaOH liquid
Stream is connected with storage tank C and is further connected with spray chamber B to realize thorough decarburization, liquid-phase outlet and the mixing chamber phase of spray chamber A
Even, another entrance input ammonium hydroxide of mixing chamber, liquid phase mixture and ammonium hydroxide hybrid reaction generation ammonium salt, the liquid-phase outlet of mixing chamber
It is connected with crystallisation chamber and realizes the coarse crystallization of ammonium salt.The gas phase entrance of spray chamber A successively with deduster, heat exchanger and gas mixing
Device connects.The gas vent of spray chamber A is connected with membrane contactor to realize the purpose using the preliminary decarburization of fresh seawater, film contact
The gaseous phase outlet of device is connected with spray chamber B flue gas inversely is contacted realization in it with the NaOH lye from diaphragm electrolysis room
Thorough decarburization, the liquid-phase outlet of membrane contactor and the liquid-phase outlet of spray chamber B are connected with storage tank D, storage tank D further with precipitation
Room connects.The gaseous phase outlet of spray chamber B is connected with chimney purified partial fume to be emptied, and another part flue gas passes through
Pipeline and drier, O2Selective absorption device connects, O2Filling O in selective absorption device2Selective absorbent carbon molecular sieve, O2
The desorption gas outlet of selective absorption device be connected with gas buffer tank, and gas buffer tank exports and before being arranged on spray chamber A
Gas mixer connects.
The operating procedure of above device comprises the following steps：
（1）Fresh seawater is subjected to filtering and impurity removing by filter, and is passed through after centrifugal pump pressurizes in RO films and realizes sea water desalination,
Wherein penetrating fluid clear water is passed through in mud chamber as output of products, seepage remaining liquid concentrated seawater through storage tank A, with from membrane contactor,
Liquid mixed precipitation in spray chamber B, will the outer row of solid precipitation, supernatant liquid be passed through in tank house electrolysis for HClO liquid streams and
NaOH liquid streams, wherein, HClO liquid streams are passed through at the top of spray chamber A through storage tank B, and NaOH liquid streams are passed through at the top of spray chamber B through storage tank C；
（2）Flue gas enters in spray chamber A after heat exchanger heat exchange and deduster carry out dedusting from spray chamber A bottoms successively, with
HClO liquid streams from tank house inversely contact the desulphurization denitration for realizing gas, and liquid product enters in mixing chamber, mixed with ammonium hydroxide
Close, adjust pH value, obtain the mixed liquor containing ammonium nitrate, ammonium sulfate and ammonium chloride；
（3）By step（2）Obtained mixed liquor obtains ammonium sulfate, ammonium nitrate and chlorination by being evaporated crystallization in crystallisation chamber
The crude product output of ammonium；
（4）Gas at the top of from spray chamber A out enters the tube side of membrane contactor, and the shell side of membrane contactor is passed through by filter mistake
Absorption occurs for the seawater of filter, the membrane component surface inside membrane contactor to realize the preliminary decarburization of gas；
（5）By step（4）Gas continue through the bottom of spray chamber B and be passed through in spray chamber B, with the NaOH liquid from tank house
The gross decarburization of gas is realized in the reverse contact of stream, and is emptied after decarburization after drier is dried by chimney, by membrane contactor
Discharge liquid and spray chamber B discharge liquid mixing after be passed through in mud chamber.
（6）Gas after desiccant dehumidification is delivered to O2To the O in gas in selective absorption device2Selective absorption, not by
The gas of absorption is passed through chimney emptying, to O after adsorption saturation2Selective absorption device carries out regeneration desorption, and the gas after desorption is defeated
Send into gas buffer tank, and continue to be passed through in the gas mixer being arranged between spray chamber A and deduster and mixed with flue gas.
The foregoing is merely highly preferred embodiment of the present invention, is not intended to limit the invention.It is all the present invention principle and
Any modification, equivalent substitution, improvement and etc. done within spirit, should be included within the scope of the present invention.
Claims (9)
1. a kind of smoke eliminator, it is characterised in that including seawater treatment system and smoke processing system；Seawater treatment system
Including sequentially connected filter, RO films, mud chamber and tank house；Smoke processing system includes sequentially connected
Spray chamber A, membrane contactor, spray chamber B, drier；Wherein, the two of spray chamber A, the absorbing liquid entrance of spray chamber B and tank house
A outlet connection, the liquid phase entrance of membrane contactor is connected with filter outlet, membrane contactor, spray chamber B liquid-phase outlet and
The concentrated seawater outlet of RO films is connected with the liquid phase entrance of mud chamber, the gas vent of spray chamber B successively with drier, chimney
Connection.
2. device according to claim 1, it is characterised in that the tank house is diaphragm electrolysis apparatus, it is electric by seawater
The NaOH liquid streams of the HClO liquid streams and alkalescence for strong oxidizing property are solved, wherein HClO fluid outlets are connected with spray chamber A, NaOH liquid streams
Outlet is connected with spray chamber B.
3. device according to claim 1, it is characterised in that between RO films and mud chamber set storage tank A, tank house and
Storage tank B is set between spray chamber A, storage tank C is set between tank house and spray chamber B, storage is set between membrane contactor and mud chamber
The liquid-phase outlet of tank D, spray chamber B are connected with storage tank D.
4. device according to claim 1, it is characterised in that centrifugal pump is set between filter and RO films.
5. device according to claim 1, it is characterised in that heat exchanger is also disposed with before gas mixer
And deduster.
6. device according to claim 1, it is characterised in that the liquid phase of the liquid-phase outlet connection mixing chamber of spray chamber A enters
Mouthful, another liquid phase entrance of mixing chamber is connected with ammonium hydroxide, and the liquid-phase outlet of mixing chamber is connected with crystallisation chamber.
7. device according to claim 1, it is characterised in that the outlet of spray chamber B is also connected with hothouse, hothouse and O2
Selective absorption device connects, O2Filling O in selective absorption device2Selective absorbent, O2The desorption gas outlet of selective absorption device
It is connected with being arranged on the gas mixer before spray chamber A.
8. a kind of flue gas purifying technique, it is characterised in that comprise the following steps：
（1）Fresh seawater is subjected to filtering and impurity removing by filter, and is passed through after centrifugal pump pressurizes in RO films and realizes sea water desalination,
Wherein penetrating fluid clear water is passed through in mud chamber as output of products, seepage remaining liquid concentrated seawater through storage tank A, with from membrane contactor,
Liquid mixed precipitation in spray chamber B, will the outer row of solid precipitation, supernatant liquid be passed through in tank house electrolysis for HClO liquid streams and
NaOH liquid streams, wherein, HClO liquid streams are passed through at the top of spray chamber A through storage tank B, and NaOH liquid streams are passed through at the top of spray chamber B through storage tank C；
（2）Flue gas enters in spray chamber A after heat exchanger heat exchange and deduster carry out dedusting from spray chamber A bottoms successively, with
HClO liquid streams from tank house inversely contact the desulphurization denitration for realizing gas, and liquid product enters in mixing chamber, mixed with ammonium hydroxide
Close, adjust pH value, obtain the mixed liquor containing ammonium nitrate, ammonium sulfate and ammonium chloride；
（3）By step（2）Obtained mixed liquor obtains ammonium sulfate, ammonium nitrate and chlorination by being evaporated crystallization in crystallisation chamber
The crude product output of ammonium；
（4）Gas at the top of from spray chamber A out enters the tube side of membrane contactor, and the shell side of membrane contactor is passed through by filter mistake
Absorption occurs for the seawater of filter, the membrane component surface inside membrane contactor to realize the preliminary decarburization of gas；
（5）By step（4）Gas continue through the bottom of spray chamber B and be passed through in spray chamber B, with the NaOH liquid from tank house
The gross decarburization of gas is realized in the reverse contact of stream, and is emptied after decarburization after drier desiccant dehumidification by chimney, and film is connect
It is passed through after the liquid mixing of liquid and spray chamber the B discharge of the discharge of tentaculum in mud chamber.
9. technique according to claim 8, it is characterised in that the technique is in step（5）Also there is step afterwards（6）By drying
Gas after dehumidifying is delivered to O2To the O in gas in selective absorption device2Selective absorption, gas not to be adsorbed are passed through cigarette
Chimney empties, to O after adsorption saturation2Selective absorption device carries out regeneration desorption, and the gas after desorption is delivered in gas buffer tank,
And continue to be passed through in the gas mixer being arranged between spray chamber A and deduster and mixed with flue gas.
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| CN201711250248.3A CN107952330A (en) | 2017-12-01 | 2017-12-01 | A kind of smoke eliminator and technique |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201711250248.3A CN107952330A (en) | 2017-12-01 | 2017-12-01 | A kind of smoke eliminator and technique |
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| CN107952330A true CN107952330A (en) | 2018-04-24 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115627487A (en) * | 2022-10-31 | 2023-01-20 | 西南石油大学 | Solar power generation and water electrolysis combined hydrogen production and building environment dehumidification system |
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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 |
| CN104190220A (en) * | 2014-08-27 | 2014-12-10 | 袁磊 | Device and method for denitrifying flue gas of coking furnace |
| CN104772028A (en) * | 2015-04-14 | 2015-07-15 | 大连海事大学 | Novel wet type ship waste gas comprehensive treatment method and device |
| CN106865840A (en) * | 2017-03-28 | 2017-06-20 | 中国科学院城市环境研究所 | A kind of ship tail gas and ballast water integrated processing system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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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 |
| CN104190220A (en) * | 2014-08-27 | 2014-12-10 | 袁磊 | Device and method for denitrifying flue gas of coking furnace |
| CN104772028A (en) * | 2015-04-14 | 2015-07-15 | 大连海事大学 | Novel wet type ship waste gas comprehensive treatment method and device |
| CN106865840A (en) * | 2017-03-28 | 2017-06-20 | 中国科学院城市环境研究所 | A kind of ship tail gas and ballast water integrated processing system |
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| CN115627487A (en) * | 2022-10-31 | 2023-01-20 | 西南石油大学 | Solar power generation and water electrolysis combined hydrogen production and building environment dehumidification system |
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