CN109395552A - A kind of liquid vapour vortex phase transformation integrated desulfurization and byproduct recovery process - Google Patents
A kind of liquid vapour vortex phase transformation integrated desulfurization and byproduct recovery process Download PDFInfo
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- CN109395552A CN109395552A CN201811364224.5A CN201811364224A CN109395552A CN 109395552 A CN109395552 A CN 109395552A CN 201811364224 A CN201811364224 A CN 201811364224A CN 109395552 A CN109395552 A CN 109395552A
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
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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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- 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
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- B01D53/34—Chemical or biological purification of waste gases
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- C01F5/40—Magnesium sulfates
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Abstract
The invention belongs to flue gas desulfurization technique fields, propose a kind of liquid vapour vortex phase transformation integrated desulfurization and byproduct recovery process, including pre- desulfurization, desulfurization, the removal of impurities of desulphurizer mixing solution, Adlerika purification, magnesium sulfate monohydrate Powder Recovery, the byproduct for solving existing flue gas desulfurization device does not obtain effective recycling technical problem.
Description
Technical field
The invention belongs to flue gas desulfurization technique field, it is related to a kind of liquid vapour vortex phase transformation integrated desulfurization and byproduct recycling
Technique.
Background technique
Sulfur dioxide in flue gas is huge to animals and plants and ecological environment harm, especially the sulfur dioxide of low concentration, by
Big in its flue gas content, harness effect is low, so it is effectively administered as a great problem for a long time.It administers in the world at present
The technical way of SO2 pollution is flue gas desulfurization.
Application No. is described in 201611117057.5 application for a patent for invention file using spraying method and equipment into
The technical solution of row desulfurization, but this method doctor solution and sulfur-containing smoke gas insufficient contact, cause desulfurization to be not thorough, and use
The device is complicated takes up a large area, without sufficiently recycling waste hot gas, waste water etc..Application No. is 201110431357.1 hairs
It is recorded in bright patent document, increases filter and dewatering screen behind the hydrocyclone of flue gas desulphurization system, use
Dewatering screen dehydration efficiently solves gypsum and is not easy dehydration problem, and product gypsum added value is high, and water is recycled, and saves and uses
Water.But only the water in sweetening process is recycled, other byproducts are not directed to.
That there are reaction efficiencies is low for existing flue gas desulfurization device, and desulfurization effect is poor, and the device is complicated, and byproduct does not obtain effectively
The technical issues of recycling, so that the energy consumption of whole system is high.
Summary of the invention
The invention proposes a kind of liquid vapour vortex phase transformation integrated desulfurization and byproduct recovery process, solve above-mentioned by-product
Product do not obtain effective recycling technical problem.
The technical scheme of the present invention is realized as follows:
A kind of liquid vapour vortex phase transformation integrated desulfurization and byproduct recovery process, comprising:
S1. magnesia dry powder desulfurizing agent is sprayed into flue, and pre- desulfurization process is carried out to sulfur-containing smoke gas；
S2. it will be passed through in desulfurizer slurry after the even gas of sulfur-containing smoke gas after pre- desulfurization and carry out desulfurization process, obtained containing miscellaneous
The magnesium sulfate mixed solution of matter, while the magnesia dry powder desulfurizing agent carried in sulfur-containing smoke gas is dissolved in desulfurizer slurry；
S3. the desulfurizer slurry droplet carried in flue gas after desulfurization is removed, atmosphere is discharged in flue gas, collects desulfurizer slurry mist
It drips and is mixed with desulfurizer slurry；
S4. it cleans to the mixed solution in S2, obtains magnesium sulfate clear liquid；
S5. the magnesium sulfate clear liquid in S4 is preheated；
S6. concentration is evaporated to the magnesium sulfate clear liquid after preheating, more water magnesium sulfates is precipitated and crystallizes and obtains the gas-liquid of water
Mixture, fixed gas and low-pressure steam；
S7. the gas-liquid mixture of water obtained in S6 step is subjected to gas-liquid separation, generates high-temperature vapor and high temperature steams
Distilled water；
S8. it will enter in S6 after the high-temperature vapor compression in S7 and magnesium sulfate clear liquid be concentrated by evaporation；
S9. the magnesium sulfate clear liquid in S5 is preheated using the hyperthermal distilled water in S7, the cooling distillation after exchanging heat
Water, which enters, prepares desulfurizer slurry in S2；
S10. magnesium sulfate clear liquid in S5 is preheated using fixed gas obtained in S6 and low-pressure steam；
S11. the crystallization of more water magnesium sulfates obtained in S6 step is dried, obtains sulfuric acid monohydrate magnesium granules, it is received
Collect and packs.
Clean as further technical solution, in S4 the following steps are included:
S41. the magnesium sulfate mixed solution containing impurity is filtered for the first time, generates just clear liquid and filter residue；
S42. secondary filter is carried out to first clear liquid, generates clear liquid and filter residue.
As further technical solution, magnesium sulfate clear liquid temperature is 50 DEG C in S4.
As further technical solution, the magnesium sulfate clear liquid temperature after preheating in S5 is 85 DEG C.
As further technical solution, the crystallization of more water magnesium sulfates is dried in S11 the following steps are included:
S111. hot wind is drawn from the cold section of outlet of ring cold machine secondary cooling zone and three；
S112. it is blended into the lower air of temperature, is mixed to form thermophilic wind with the hot wind in S101；
S113. by thermophilic wind dust removal by filtration, clean thermophilic wind is formed；
S114. more water magnesium sulfates are dried using thermophilic wind clean in S103.
Compared with prior art, it working principle of the present invention and has the beneficial effect that
1, the present invention in, flue gas desulfurization technique process use magnesia and magnesium hydroxide as desulfurizing agent to sulfur-containing smoke gas into
Row desulphurization reaction, desulphurization reaction equipment be followed successively by from top to bottom chimney, combination except fog chamber, vortex phase transformation reaction device, equal gas chamber,
Integrated collecting tank, each equipment are connected by pipeline, and sulfur-containing smoke gas enters equal device of air from chimney, full of after equal device of air to
Vortex desulphurization reaction is carried out in upper entrance vortex phase transformation reaction device, the flue gas after desulfurization carries part reacting slurry droplet, into
Enter except fog chamber is separated into no sulphur flue gas and reacting slurry, no sulphur flue gas is discharged atmosphere, and reacting slurry is collected and returns to
In integrated collecting tank.Dry powder-shaped desulfurizing agent injection dress is additionally provided with from the pipeline that chimney enters equal gas chamber in sulfur-containing smoke gas
It sets, dry powder desulfurizing agent is sprayed into pipeline and is used to carry out the pre- desulfurization of initial reaction with sulfur-containing smoke gas, this only partially contains in the process
Sulphur flue gas is desulfurized, and also only part dry powder desulfurizing agent generation effect is reacted, and unreacted dry powder desulfurizing agent is with flue gas
Into equal gas chamber, a part of dry powder desulfurizing agent is advanced into vortex phase transformation reaction device with flue gas from equal gas chamber, and there are also one
Part dry powder desulfurizing agent is fallen in integrated collecting tank under equal gas chamber, and integrated collecting tank is to be used to prepare desulphurization reaction slurry
Liquid, the desulphurization reaction slurries prepared are input in vortex phase transformation reaction device, therefore whether enter vortex phase transformation reaction dress
It is dense that dry powder desulfurizing agent in setting still all plays increase desulphurization reaction slurries into the dry powder desulfurizing agent in integrated collecting tank
The effect and effect of degree.Therefore the dry powder desulfurizing agent realizes preliminary desulfurization and prepares the double action of desulfurizer slurry simultaneously.
The sulfur content in sulfur-containing smoke gas by desulfurization twice is also extremely low, basic environmental sound.One integrated collecting tank can be with
Realize slurrying, loop slurry and sediment slurry.Space is saved, while saving cost, slurries energy conservation and environmental protection can be recycled,
Desulfurization effect is more preferable.
2, it in the present invention, is produced in the reactive desulfurizing agent slurries after being reacted with sulfur-containing smoke gas miscellaneous based on magnesium sulfate
Matter, the time, which has been grown, will lead to desulfurization effect variation, it is therefore desirable to will be vortexed the desulfurizing agent containing impurity in phase transformation reaction device
Reacting slurry discharge, and carries out purified filter, byproduct magnesium sulfate can industrially be used for process hides, explosive, fertilizer, papermaking,
The industry such as porcelain, printing and dyeing material, lead-acid accumulator, agriculturally for improveing soil quality.It therefore can be by the sulfuric acid in impurity
Magnesium carries out concentration purification and is sulfuric acid magnesium granules and packs sale, on the one hand reduces the discharge of impure desulphurization reaction slurries, separately
On the one hand the byproduct can also be recycled and obtains economic benefit.
3, in the present invention, impurity main source has desulfurizing agent impurity, flue gas to hold under the arm in the desulphurization reaction slurries containing magnesium sulfate
Calcium ions and magnesium ions, magnesium sulfite sediment and the insoluble matters such as part of sulfuric acid calcium and silica etc. in the dust of band, process water, choosing
With membrane pressure filter and double filtration system is set, i.e., the slurries containing impurity are squeezed into filter press template using high-pressure pump
Between, slurries are first squeezed using the high pressure of pump, filter cloth rear impurity of the high pressure slurries Jing Guo high mesh number is kept off by filter cloth
Between filter press template, and the slurries squeezed out become clear liquid from script turbid solution and flow into storage bin, when high-pressure pump is fed to one
When rear slurry impurity of fixing time is essentially filled with gap between template, starting twice pressing pump handle impurity carries out secondary extrusion and is formed
Impurity flitch again squeezes the free water between impurity and increases clear liquid yield.Magnesium sulfate intermediate fluid flows into clear after a time filtering
Liquid storage bin squeezes into the secondary removal of impurities processing of No. two high detailed catalogue filter press progress by high-pressure pump again after carrying out heat preservation storage, carries out same
Enter magnesium sulfate clear liquid storage bin after sample step and carries out heat preservation storage waiting follow-up equipment charging.Magnesium sulfate clear liquid passes through distilled water
Plate heat exchanger is preheated using fixed gas plate heat exchanger and steam-plate type heat exchanger, mainly the temperature of clear liquid
85 DEG C or so are increased to by 50 DEG C, reduces power consumption and the clear liquid concentrate time of whole system.
4, it in the present invention, is warming up to 85 DEG C of Adlerika and enters and carry out heating evaporation in crystallizing evaporator, evaporation knot
Brilliant device arrival end and outlet end are each provided with a forced-circulation evaporator, and initial steam is filled into forced-circulation evaporator and carried out clearly
Liquid heating, the clear liquid by heating squeeze into crystallizing evaporator by circulating pump, and concentrate is evaporated under high-temperature low-pressure environment, and water steams
Gas is separated to distillation water pot and then is passed through distilled water pump and squeeze into distilled water plate heat exchanger and preheated by knockout drum,
The fixed gas and low-pressure steam being discharged in forced-circulation evaporator respectively enter fixed gas plate heat exchanger and steam-plate type heat exchange
Adlerika is preheated in device, is back to liquid into the distilled water after progress heat exchange in distilled water plate heat exchanger
Vapour is vortexed slurrying in phase transformation integrated desulfurization device, is also able to achieve zero waste liquid outlet and reduction while realizing heat recovery and utilization
The purpose of clear water usage amount.The fixed gas in evaporating concentration process and low-pressure steam are also utilized simultaneously.
5, in the present invention, after purification is concentrated in Adlerika in crystallizing evaporator, the density of concentrate reaches material analysis
Out when condition, material is squeezed into progress crystal precipitation in material crystallizing tank by discharging pump and is grown up, is then beaten by dispensing valve
Enter vacuum belt dewaterer, using water-ring vacuum pump negative pressure is pumped between belt and filter cloth, high-temperature material is taken out by negative pressure
Cool down after water and become more water magnesium sulfates crystallization carnallites, there are also 15% or so water content in crystal at this moment, then utilize ring
Cold two, three cold sections of hot winds are dried in flash vessel, take away free water and uncalled crystal water in carnallite, the heat after heat exchange
Wind carries sulfuric acid monohydrate magnesium granules secretly and carries out material recycle by whirlwind collector and cloth bag collector, and uses device of full automatic packaging
Carry out material filling packaging suture hot melt.
6, in the present invention, phase transformation integrated desulfurization and byproduct recovery process are vortexed by above-mentioned liquid vapour, realizing sulfur-bearing
After the desulfurization process of flue gas, moreover it is possible to the impurity magnesium sulfate in reacting slurry in the process be carried out crystallization recycling, while will distillation
Water, hot steam, fixed gas and ring cold machine exhaust gas be introduced into the equipment in technique and be recycled, greatly reduce
Sulfur content, the usage amount of water, the usage amount of thermal energy of the flue gas of discharge, reduce waste discharge, while reducing environmental pollution
It can also additional income.
7, in the present invention, the reacting slurry by the vortex phase transformation integrated desulfurization device desulfurization of liquid vapour carries out removal of impurities purification again
Isothermal holding is carried out in deposit clear liquid holding vessel afterwards, the clear liquid temperature general control is at 50 DEG C or so.It is too fast to can be avoided clear liquid
Precipitating.Fixed gas, high-temperature steam are all at 100 DEG C, and the temperature of magnesium sulfate clear liquid is not more than 100 DEG C after heat exchange, and
Temperature is excessively high to make magnesium sulfate clear liquid begin to evaporation process outside crystallizing evaporator, start magnesium sulfate in plate heat exchanger
Concentration is easy blocking plate heat exchanger.85 DEG C are generally kept in, can be fully warmed-up, saves and is concentrated by evaporation the time.
8, in the present invention, ring cold machine two, three cold sections of hot blast temperatures reach 200 DEG C -320 DEG C, are passed by sirocco reclamation pipeline
It send, opens cold wind valve, the introducing lower air of temperature is mixed with hot wind to be cooled down, and (uses market by temperature sensor
Upper commercially available temperature sensor) monitoring temperature variation, reach and meets to aqueous MgSO4(160 after the temperature that solid is dried
DEG C or so), mixed gas enters in electrostatic precipitator, and the dust impurity in mixed gas is filtered, mixed after filtering
Gas is closed to enter in rotary flash evaporator by the air outlet of the first air-introduced machine to MgSO4Solid is dried, in material
Free water drying and a part of more water magnesium sulfates are baked magnesium sulfate monohydrate, then in the case where the draft of the second air-introduced machine acts on,
Hot wind enters whirlwind collector with powdery sulfuric acid monohydrate magnesium granules, by dry powdery magnesium sulfate monohydrate under whirlwind collector
The collector of side exports discharge, and gas enters cloth bag collector from collector air outlet and carries out secondary siccative recycling, siccative from
Cloth bag discharge port discharge below cloth bag collector, the siccative that whirlwind collector and cloth bag collector are collected all enter storage in feed bin
It deposits, is discharged into atmosphere without dusty gas after secondary recovery siccative, realizes the recycling of ring cold machine high temperature exhaust gas.This
Sirocco reclamation not only greatly reduces the purpose that energy consumption has also achieved energy-saving and emission-reduction using device, and ring cold machine hot wind does not have not only
Atmosphere pollution will not also have an impact main line.
9, in the present invention, flue gas desulfurization is carried out using liquid vapour vortex desulfurizer, compared to traditional spray sulfur method
Cost can be saved, and discharges sulfur content in flue gas and is much smaller than traditional spray sulfur method.
Applicant's innovative design flue gas desulfurization and subsequent byproduct recovery process, by technique output it is all kinds of
Byproduct is recycled, sulfur content in the flue gas after not only greatly reducing desulfurization process, improves desulfurization process effect
Rate also reduces the external heat source and raw material inputted into entire process flow, improves product utilization rate.
10, in the present invention, Powderjet device is used for magnesia dry powder desulfurizing agent with certain jet velocity and ejection
Amount, which sprays into, carries out pre- desulfurization in flue gas transmission pipeline, Powderjet device includes the disk being fixedly connected with pipeline, is opened on disk
There is a circular through hole, the opening on circular through hole and pipeline is interconnected, and turntable is provided with above disk, if offering on turntable
Dry for holding the charge slot of magnesia dry powder.Other end blowing constantly into charge slot above turntable, according in pipeline
The concentration of sulfur-containing smoke gas can control the amount of blowing, and then turntable constantly rotates, and since turntable is stopped by the disk of bottom, make object
Material can only can just enter in flue rotating at circular through hole, and the negative pressure in flue can suck material, from
And it is reacted with sulfur-containing smoke gas and carries out pre- desulfurization.When the charge slot on the circular through hole and turntable being connected to flue rushes to,
Material drops downward into pipeline, and after material is entirely fallen in pipeline, turntable seals circular through hole just, avoids the flue gas in pipeline
Evolution.
Detailed description of the invention
The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.
Fig. 1 is present invention process flow diagram；
Fig. 2 is secondary impurity removing process schematic diagram in the present invention；
Fig. 3 is Powderjet device schematic perspective view in the present invention；
Fig. 4 is Powderjet device schematic view of the front view in the present invention；
Fig. 5 is disc structure schematic diagram in the present invention；
Fig. 6 is turntable structural schematic diagram of the present invention.
In figure: 1- turntable, 11- charge slot, 12- rotary shaft, 13- gear, 14- annular protrusion, 2- disk, 21- circle are logical
Hole, 22- annular groove, 3- motor, 4- feeding warehouse, 51- air pump, 52- tracheae, 53- air pump jet port, 6- shell, 7- pipeline.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
As shown in figs 1 to 6, the present invention proposes that a kind of liquid vapour is vortexed phase transformation integrated desulfurization and byproduct recovery process, packet
It includes:
S1. magnesia dry powder desulfurizing agent is sprayed into flue, and pre- desulfurization process is carried out to sulfur-containing smoke gas；
S2. it will be passed through in desulfurizer slurry after the even gas of sulfur-containing smoke gas after pre- desulfurization and carry out desulfurization process, obtained containing miscellaneous
The magnesium sulfate mixed solution of matter, while the magnesia dry powder desulfurizing agent carried in sulfur-containing smoke gas is dissolved in desulfurizer slurry；
S3. the desulfurizer slurry droplet carried in flue gas after desulfurization is removed, atmosphere is discharged in flue gas, collects desulfurizer slurry mist
It drips and is mixed with desulfurizer slurry；
S4. it cleans to the mixed solution in S2, obtains magnesium sulfate clear liquid；
S5. the magnesium sulfate clear liquid in S4 is preheated；
S6. concentration is evaporated to the magnesium sulfate clear liquid after preheating, more water magnesium sulfates is precipitated and crystallizes and obtains the gas-liquid of water
Mixture, fixed gas and low-pressure steam；
S7. the gas-liquid mixture of water obtained in S6 step is subjected to gas-liquid separation, generates high-temperature vapor and high temperature steams
Distilled water；
S8. it will enter in S6 after the high-temperature vapor compression in S7 and magnesium sulfate clear liquid be concentrated by evaporation；
S9. the magnesium sulfate clear liquid in S5 is preheated using the hyperthermal distilled water in S7, the cooling distillation after exchanging heat
Water, which enters, prepares desulfurizer slurry in S2；
S10. magnesium sulfate clear liquid in S5 is preheated using fixed gas obtained in S6 and low-pressure steam；
S11. the crystallization of more water magnesium sulfates obtained in S6 step is dried, obtains sulfuric acid monohydrate magnesium granules, it is received
Collect and packs.
In the present embodiment, flue gas desulfurization technique process use magnesia and magnesium hydroxide as desulfurizing agent to sulfur-containing smoke gas into
Row desulphurization reaction, desulphurization reaction equipment be followed successively by from top to bottom chimney, combination except fog chamber, vortex phase transformation reaction device, equal gas chamber,
Integrated collecting tank, each equipment are connected by pipeline, and sulfur-containing smoke gas enters equal device of air from chimney, full of after equal device of air to
Vortex desulphurization reaction is carried out in upper entrance vortex phase transformation reaction device, the flue gas after desulfurization carries part reacting slurry droplet, into
Enter except fog chamber is separated into no sulphur flue gas and reacting slurry, no sulphur flue gas is discharged atmosphere, and reacting slurry is collected and returns to
In integrated collecting tank.
In the present embodiment, the injection of dry powder-shaped desulfurizing agent is additionally provided with from the pipeline that chimney enters equal gas chamber in sulfur-containing smoke gas
Device sprays dry powder desulfurizing agent into pipeline and is used to carry out the pre- desulfurization of initial reaction with sulfur-containing smoke gas, this only has part in the process
Sulfur-containing smoke gas is desulfurized, and also only part dry powder desulfurizing agent generation effect is reacted, and unreacted dry powder desulfurizing agent is with cigarette
Gas enters equal gas chamber, and a part of dry powder desulfurizing agent is advanced into vortex phase transformation reaction device with flue gas from equal gas chamber, also
A part of dry powder desulfurizing agent is fallen in integrated collecting tank under equal gas chamber, and integrated collecting tank is to be used to prepare desulphurization reaction slurry
Liquid, the desulphurization reaction slurries prepared are input in vortex phase transformation reaction device, therefore whether enter vortex phase transformation reaction dress
It is dense that dry powder desulfurizing agent in setting still all plays increase desulphurization reaction slurries into the dry powder desulfurizing agent in integrated collecting tank
The effect and effect of degree.Therefore the dry powder desulfurizing agent realizes preliminary desulfurization and prepares the double action of desulfurizer slurry simultaneously.
The sulfur content in sulfur-containing smoke gas by desulfurization twice is also extremely low, basic environmental sound.One integrated collecting tank can be with
Realize slurrying, loop slurry and sediment slurry.Space is saved, while saving cost, slurries energy conservation and environmental protection can be recycled,
Desulfurization effect is more preferable.
In the present embodiment, produced in the reactive desulfurizing agent slurries after being reacted with sulfur-containing smoke gas miscellaneous based on magnesium sulfate
Matter, the time, which has been grown, will lead to desulfurization effect variation, it is therefore desirable to will be vortexed the desulfurizing agent containing impurity in phase transformation reaction device
Reacting slurry discharge, and carries out purified filter, byproduct magnesium sulfate can industrially be used for process hides, explosive, fertilizer, papermaking,
The industry such as porcelain, printing and dyeing material, lead-acid accumulator, agriculturally for improveing soil quality.It therefore can be by the sulfuric acid in impurity
Magnesium carries out concentration purification and is sulfuric acid magnesium granules and packs sale, on the one hand reduces the discharge of impure desulphurization reaction slurries, separately
On the one hand the byproduct can also be recycled and obtains economic benefit.
In the present embodiment, impurity main source has desulfurizing agent impurity, flue gas to hold under the arm in the desulphurization reaction slurries containing magnesium sulfate
Calcium ions and magnesium ions, magnesium sulfite sediment and the insoluble matters such as part of sulfuric acid calcium and silica etc. in the dust of band, process water, choosing
With membrane pressure filter and double filtration system is set, i.e., the slurries containing impurity are squeezed into filter press template using high-pressure pump
Between, slurries are first squeezed using the high pressure of pump, filter cloth rear impurity of the high pressure slurries Jing Guo high mesh number is kept off by filter cloth
Between filter press template, and the slurries squeezed out become clear liquid from script turbid solution and flow into storage bin, when high-pressure pump is fed to one
When rear slurry impurity of fixing time is essentially filled with gap between template, starting twice pressing pump handle impurity carries out secondary extrusion and is formed
Impurity flitch again squeezes the free water between impurity and increases clear liquid yield.Magnesium sulfate intermediate fluid flows into clear after a time filtering
Liquid storage bin squeezes into the secondary removal of impurities processing of No. two high detailed catalogue filter press progress by high-pressure pump again after carrying out heat preservation storage, carries out same
Enter magnesium sulfate clear liquid storage bin after sample step and carries out heat preservation storage waiting follow-up equipment charging.
In the present embodiment, magnesium sulfate clear liquid passes through distilled water plate heat exchanger, using fixed gas plate heat exchanger and steaming
Vapour plate heat exchanger is preheated, and the temperature of clear liquid is mainly increased to 85 DEG C or so by 50 DEG C, reduces whole system
Power consumption and clear liquid concentrate time.
In the present embodiment, it is warming up to 85 DEG C of Adlerika and enters and carry out heating evaporation in crystallizing evaporator, evaporation knot
Brilliant device arrival end and outlet end are each provided with a forced-circulation evaporator, and initial steam is filled into forced-circulation evaporator and carried out clearly
Liquid heating, the clear liquid by heating squeeze into crystallizing evaporator by circulating pump, and concentrate is evaporated under high-temperature low-pressure environment, and water steams
Gas is separated to distillation water pot and then is passed through distilled water pump and squeeze into distilled water plate heat exchanger and preheated by knockout drum,
The fixed gas and low-pressure steam being discharged in forced-circulation evaporator respectively enter fixed gas plate heat exchanger and steam-plate type heat exchange
Adlerika is preheated in device, is back to liquid into the distilled water after progress heat exchange in distilled water plate heat exchanger
Vapour is vortexed slurrying in phase transformation integrated desulfurization device, is also able to achieve zero waste liquid outlet and reduction while realizing heat recovery and utilization
The purpose of clear water usage amount.The fixed gas in evaporating concentration process and low-pressure steam are also utilized simultaneously.
In the present embodiment, after purification is concentrated in Adlerika in crystallizing evaporator, the density of concentrate reaches material analysis
Out when condition, material is squeezed into progress crystal precipitation in material crystallizing tank by discharging pump and is grown up, is then beaten by dispensing valve
Enter vacuum belt dewaterer, using water-ring vacuum pump negative pressure is pumped between belt and filter cloth, high-temperature material is taken out by negative pressure
Cool down after water and become more water magnesium sulfates crystallization carnallites, there are also 15% or so water content in crystal at this moment, then utilize ring
Cold two, three cold sections of hot winds are dried in flash vessel, take away free water and uncalled crystal water in carnallite, the heat after heat exchange
Wind carries sulfuric acid monohydrate magnesium granules secretly and carries out material recycle by whirlwind collector and cloth bag collector, and uses device of full automatic packaging
Carry out material filling packaging suture hot melt.
In the present embodiment, phase transformation integrated desulfurization and byproduct recovery process are vortexed by above-mentioned liquid vapour, realizing sulfur-bearing
After the desulfurization process of flue gas, moreover it is possible to the impurity magnesium sulfate in reacting slurry in the process be carried out crystallization recycling, while will distillation
Water, hot steam, fixed gas and ring cold machine exhaust gas be introduced into the equipment in technique and be recycled, greatly reduce
Sulfur content, the usage amount of water, the usage amount of thermal energy of the flue gas of discharge, reduce waste discharge, while reducing environmental pollution
It can also additional income.
Further, in S4 removal of impurities the following steps are included:
S41. the magnesium sulfate mixed solution containing impurity is filtered for the first time, generates just clear liquid and filter residue；
S42. secondary filter is carried out to first clear liquid, generates clear liquid and filter residue.
Further, magnesium sulfate clear liquid temperature is 50 DEG C in S4.
In the present embodiment, the reacting slurry by the vortex phase transformation integrated desulfurization device desulfurization of liquid vapour carries out removal of impurities purification again
Isothermal holding is carried out in deposit clear liquid holding vessel afterwards, the clear liquid temperature general control is at 50 DEG C or so.It is too fast to can be avoided clear liquid
Precipitating.
Further, the magnesium sulfate clear liquid temperature after preheating in S5 is 85 DEG C.
In the present embodiment, the temperature of magnesium sulfate clear liquid is not yet all at 100 DEG C, after heat exchange for fixed gas, high-temperature steam
It can be more than 100 DEG C, and temperature is excessively high that magnesium sulfate clear liquid can be made to begin to evaporation process outside crystallizing evaporator, make magnesium sulfate in plate
Start to be concentrated in formula heat exchanger, is easy blocking plate heat exchanger.85 DEG C are generally kept in, can be fully warmed-up, it is dense to save evaporation
The contracting time.
Further, the crystallization of more water magnesium sulfates is dried in S11 the following steps are included:
S111. hot wind is drawn from the cold section of outlet of ring cold machine secondary cooling zone and three；
S112. it is blended into the lower air of temperature, is mixed to form thermophilic wind with the hot wind in S101；
S113. by thermophilic wind dust removal by filtration, clean thermophilic wind is formed；
S114. more water magnesium sulfates are dried using thermophilic wind clean in S103.
In the present embodiment, ring cold machine two, three cold sections of hot blast temperatures reach 200 DEG C -320 DEG C, are passed by sirocco reclamation pipeline
It send, opens cold wind valve, the introducing lower air of temperature is mixed with hot wind to be cooled down, and (uses market by temperature sensor
Upper commercially available temperature sensor) monitoring temperature variation, reach and meets to aqueous MgSO4(160 after the temperature that solid is dried
DEG C or so), mixed gas enters in electrostatic precipitator, and the dust impurity in mixed gas is filtered, mixed after filtering
Gas is closed to enter in rotary flash evaporator by the air outlet of the first air-introduced machine to MgSO4Solid is dried, in material
Free water drying and a part of more water magnesium sulfates are baked magnesium sulfate monohydrate, then in the case where the draft of the second air-introduced machine acts on,
Hot wind enters whirlwind collector with powdery sulfuric acid monohydrate magnesium granules, by dry powdery magnesium sulfate monohydrate under whirlwind collector
The collector of side exports discharge, and gas enters cloth bag collector from collector air outlet and carries out secondary siccative recycling, siccative from
Cloth bag discharge port discharge below cloth bag collector, the siccative that whirlwind collector and cloth bag collector are collected all enter storage in feed bin
It deposits, is discharged into atmosphere without dusty gas after secondary recovery siccative, realizes the recycling of ring cold machine high temperature exhaust gas.This
Sirocco reclamation not only greatly reduces the purpose that energy consumption has also achieved energy-saving and emission-reduction using device, and ring cold machine hot wind does not have not only
Atmosphere pollution will not also have an impact main line.
Comparative example one: carrying out flue gas desulfurization processing using spray desulfurizer, takes off by doctor solution atomization, with smoke contacts
Byproduct is collected and made to doctor solution after sulphur, reaction, as a result as follows:
| Project | Consumption | Expense (Wan Yuan) |
| Sodium hydroxide etc. | 680(t) | -408 |
| Electricity | 6.5*106(KWh) | -325 |
| Water | 13250(t) | -4.63 |
| Steam | 900(t) | -5.4 |
| Annual cost is total | -743.03 |
SO in flue gas2Initial concentration is 2000mg/Nm3, SO in the flue gas that is discharged after desulfurization2Concentration is 160mg/
Nm3, discharge standard 200mg/Nm newest lower than country3, expend 743.03 ten thousand yuan year.
Embodiment one:
SO in flue gas2Initial concentration is 2000mg/Nm3, desulfurization and pair are carried out according to S1-S11, S41-S42, S111-S114
Product recycling, SO in the flue gas discharged after desulfurization2Concentration is 45mg/Nm3, lower than concentration 160mg/Nm in comparative example one3。
| Project | Consumption | Expense (Wan Yuan) |
| Magnesium oxide powder | 800(t) | 560 |
| Electricity | 3.125*105(KWh) | 152 |
| Water | 5650(t) | 2 |
| Steam | 920(t) | 5.52 |
| Annual cost is total | -719.52 |
Magnesium oxide powder usage amount is 800 tons, and electric usage amount is 3.125x105Kilowatt hour, 5650 tons of water usage amount, steam
920 tons of usage amount, 840 tons of byproduct magnesium sulfate monohydrate powder weight is obtained, is calculated with 2400 yuan/ton of market price, profit 201.6 ten thousand
Member, annual cost add up to 517.9 ten thousand yuan, save 225.13 ten thousand yuan in total compared to comparative example one.
Embodiment two:
S1 is not used, directly reacts sulfur-containing smoke gas with desulfurizer slurry, other steps are identical, as a result as follows: in flue gas
SO2Initial concentration is 2000mg/Nm3, SO in the flue gas that is discharged after desulfurization2Concentration is 65mg/Nm3, lower than the newest row of country
Put standard 200mg/Nm3, magnesium oxide powder usage amount is 800 tons, and electric usage amount is 3.125x105Kilowatt hour, water usage amount 5650
Ton, 920 tons of steam usage amount, the weight for obtaining byproduct sulfuric acid monohydrate magnesium dust is 840 tons, is made a profit 201.6 ten thousand yuan, annual cost
Add up to 517.9 ten thousand yuan.
Removal step only carries out once in embodiment three: S4, other steps are the same as example 1, as a result as follows: flue gas
Middle SO2Initial concentration is 2000mg/Nm3, SO in the flue gas that is discharged after desulfurization2Concentration is 45mg/Nm3, magnesium oxide powder makes
Dosage is 800 tons, and electric usage amount is 3.125x105Kilowatt hour, 920 tons of steam usage amount, obtains by-product by 5650 tons of water usage amount
The weight of product sulfuric acid monohydrate magnesium dust is 800 tons, is made a profit 1,920,000 yuan, annual cost adds up to 527.52 ten thousand yuan.
Example IV: without the preheating step of S5, other steps are the same as example 1, as a result as follows: SO in flue gas2
Initial concentration is 2000mg/Nm3, magnesium oxide powder usage amount is 800 tons, SO in the flue gas discharged after desulfurization2Concentration is
45mg/Nm3, electric usage amount is 4.0x105Kilowatt hour, expense 2,000,000；5650 tons of water usage amount, 1000 tons of steam usage amount, take
With 60,000, the weight for obtaining byproduct sulfuric acid monohydrate magnesium dust is 840 tons, is made a profit 201.6 ten thousand yuan, annual cost adds up to 566.4 ten thousand
Member.
It is preheated in embodiment five: S5 using initial steam, other steps are the same as example 1, as a result as follows: flue gas
Middle SO2Initial concentration is 2000mg/Nm3, SO in the flue gas that is discharged after desulfurization2Concentration is 45mg/Nm3, magnesium oxide powder makes
Dosage is 800 tons, and electric usage amount is 3.125x105Kilowatt hour, 1390 tons of steam usage amount, obtains secondary by 5650 tons of water usage amount
The weight of product sulfuric acid monohydrate magnesium dust is 800 tons, is made a profit 1,920,000 yuan, annual cost amounts to 532.34 ten thousand yuan.
In conclusion flue gas desulfurization is carried out using liquid vapour vortex desulfurizer, compared to traditional spray sulfur method energy
Cost is enough saved, and discharges sulfur content in flue gas and is much smaller than traditional spray sulfur method.
Applicant's innovative design flue gas desulfurization and subsequent byproduct recovery process, by technique output it is all kinds of
Byproduct is recycled, sulfur content in the flue gas after not only greatly reducing desulfurization process, improves desulfurization process effect
Rate also reduces the external heat source and raw material inputted into entire process flow, improves product utilization rate.
Further, magnesia dry powder desulfurizing agent, powderject are sprayed into flue using Powderjet device in S1
Device includes the turntable 1 of the rotary setting above flue gas transmission pipeline, and 1 bottom of turntable is provided with circle identical with 1 diameter of turntable
Disk 2 is provided with circular through hole 21 on disk 2, and circular through hole 21 is connected to flue, if being evenly arranged in 1 circumferential direction of turntable
Dry charge slot 11.
In the present embodiment, Powderjet device is used for magnesia dry powder desulfurizing agent with certain jet velocity and spray volume
It sprays into and carries out pre- desulfurization in flue gas transmission pipeline 7, Powderjet device includes the disk 2 being fixedly connected with pipeline 7, on disk 2
It is provided with a circular through hole 21, the opening on circular through hole 21 and pipeline 7 is interconnected, and turntable 1, turntable 1 are provided with above disk 2
On offer several for holding the charge slot 11 of magnesia dry powder.The square other end is constantly into charge slot 11 on the turntable 1
Blowing can control the amount of blowing according to the concentration of sulfur-containing smoke gas in pipeline 7, and then turntable 1 constantly rotates, due to 1 quilt of turntable
The disk 2 of bottom stops, and enter material can only just in flue rotating at circular through hole 21, in flue 7
Negative pressure material can be sucked, carry out pre- desulfurization to react with sulfur-containing smoke gas.When the circular through hole being connected to flue 7
21 with the charge slot 11 on turntable 1 when rushing to, and material drops downward into pipeline 7, and after material is entirely fallen in pipeline 7, turntable 1 is proper
Circular through hole 21 is sealed well, and the flue gas in pipeline 7 is avoided to escape.
Further, it is provided with rotary shaft 12 on 1 axis of turntable, gear 13, rotary shaft 12 is coaxially arranged in rotary shaft 12
Side is provided with rotating electric machine 3, and motor 3 is connect by chain with the gear 13 in rotary shaft 12.
In the present embodiment, it is coaxially connected with rotary shaft 12 at the center of turntable 1, is provided with gear in rotary shaft 12, is turning
1 side of disk is provided with motor 3, and gear 13 is also equipped on the output shaft of motor 3, and motor 3 is revolved by chain-driving rotary shaft 12
Turn.
Further, charge slot 11 is cylindrical, and 21 diameter of circular through hole is equal with the diameter of charge slot 11, circular through hole 21
Only one.
In the present embodiment, charge slot 11 is cylinder-shaped, and 21 diameter of circular through hole on the diameter of charge slot 11 and disk 2
It is identical, material can be made smoothly to enter in flue 7, and reduce material and be stuck in charge slot 11 or turntable 1 and disk 2
Between gap in amount.Circular through hole 21 are arranged one, it is contemplated that pipeline 7 opened hole excessively and will increase flue gas evolution can
Energy property, and the inventory of a charge slot 11 can control, and can satisfy the inventory that pre- desulphurization reaction needs.
Further, disk 2 is provided with annular groove 22 close to the edge of the side of turntable 1, and 1 bottom of turntable is provided with card
Enter the annular protrusion 14 in annular groove 22.
In the present embodiment, it is provided with annular groove 22 on disk 2, annular protrusion 14, annular protrusion 14 are provided on turntable 1
It is rotated in annular groove 22, since charge slot 11 is the straight barrel type structure being open up and down, annular groove 22 and annular is set
Protrusion 14 can reduce the amount that material is discharged from disk 2 and the circumferential gap of turntable 1.
Further, air pump jet port 53 is provided with right above circular through hole 21, air pump jet port 53 is located at 1 top of turntable.
In the present embodiment, the top of turntable 1 is provided with air pump jet port 53, and air pump jet port 53 is located at the circle on disk 2
Right above shape through-hole 21, air pump jet port 53 connects air pump 51 by tracheae 52, and setting air pump 51 can make material enter pipeline 7
Interior speed is bigger, is injected into pipeline 7 and with the collision of 7 inner wall of pipeline is easier that material is made to scatter later, increases material and sulfur-bearing cigarette
The contact area of gas improves pre- desulfurization effect.
Further, feeding warehouse 4 is provided with above disk 2,4 bottom opening of feeding warehouse is equal with 21 diameter of circular through hole.
In the present embodiment, feeding warehouse 4 is provided with above disk 2, feeding warehouse 4 is arranged far from the side of air pump jet port 5,
Feeding warehouse 4 can continuously be each 11 blowing of charge slot, and can control the amount that material is released, section by devices such as concussion disks
Less manpower blowing.Feeding warehouse 4 can connect the device of bigger storage material.
Further, shell 6 is provided with outside feeding warehouse 4, turntable, disk 2, motor 3.
In the present embodiment, shell 6 is escaped for reducing material dust.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (5)
1. a kind of liquid vapour vortex phase transformation integrated desulfurization and byproduct recovery process, which comprises the following steps:
S1. magnesia dry powder desulfurizing agent is sprayed into flue, and pre- desulfurization process is carried out to sulfur-containing smoke gas；
S2. it will be passed through in desulfurizer slurry after the even gas of sulfur-containing smoke gas after pre- desulfurization and carry out desulfurization process, obtained containing impurity
Magnesium sulfate mixed solution, while the magnesia dry powder desulfurizing agent carried in sulfur-containing smoke gas is dissolved in desulfurizer slurry；
S3. the desulfurizer slurry droplet carried in flue gas after desulfurization is removed, atmosphere is discharged in flue gas, collects desulfurizer slurry droplet simultaneously
It is mixed with desulfurizer slurry；
S4. it cleans to the mixed solution in S2, obtains magnesium sulfate clear liquid；
S5. the magnesium sulfate clear liquid in S4 is preheated；
S6. concentration is evaporated to the magnesium sulfate clear liquid after preheating, more water magnesium sulfates is precipitated and crystallizes and obtains the gas-liquid mixed of water
Object, fixed gas and low-pressure steam；
S7. the gas-liquid mixture of water obtained in S6 step is subjected to gas-liquid separation, generates high-temperature vapor and hyperthermal distilled water；
S8. it will enter in S6 after the high-temperature vapor compression in S7 and magnesium sulfate clear liquid be concentrated by evaporation；
S9. the magnesium sulfate clear liquid in S5 is preheated using the hyperthermal distilled water in S7, the cooling distilled water after exchanging heat into
Enter and prepares desulfurizer slurry in S2；
S10. magnesium sulfate clear liquid in S5 is preheated using fixed gas obtained in S6 and low-pressure steam；
S11. the crystallization of more water magnesium sulfates obtained in S6 step is dried, obtains sulfuric acid monohydrate magnesium granules, it is collected simultaneously
Packaging.
2. a kind of liquid vapour vortex phase transformation integrated desulfurization according to claim 1 and byproduct recovery process, feature exist
In, in S4 removal of impurities the following steps are included:
S41. the magnesium sulfate mixed solution containing impurity is filtered for the first time, generates just clear liquid and filter residue；
S42. secondary filter is carried out to first clear liquid, generates clear liquid and filter residue.
3. a kind of liquid vapour vortex phase transformation integrated desulfurization according to claim 2 and byproduct recovery process, feature exist
In magnesium sulfate clear liquid temperature is 50 DEG C in S4.
4. a kind of liquid vapour vortex phase transformation integrated desulfurization according to claim 3 and byproduct recovery process, feature exist
In the magnesium sulfate clear liquid temperature after preheating in S5 is 85 DEG C.
5. a kind of liquid vapour vortex phase transformation integrated desulfurization according to claim 4 and byproduct recovery process, feature exist
In, the crystallization of more water magnesium sulfates is dried in S11 the following steps are included:
S111. hot wind is drawn from the cold section of outlet of ring cold machine secondary cooling zone and three；
S112. it is blended into the lower air of temperature, is mixed to form thermophilic wind with the hot wind in S101；
S113. by thermophilic wind dust removal by filtration, clean thermophilic wind is formed；
S114. more water magnesium sulfates are dried using thermophilic wind clean in S103.
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Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2665245A1 (en) * | 1990-07-27 | 1992-01-31 | Entropie Sa | Unit for concentrating a heat-sensitive solution, in particular grape must |
| JPH10109013A (en) * | 1996-10-04 | 1998-04-28 | Hisaji Koyama | Magnesium oxide and regenerated sulfuric acid recovering type flue gas desulfurization apparatus |
| US20040018133A1 (en) * | 2002-07-23 | 2004-01-29 | Radway Jerrold E. | Combustion emissions control and utilization of byproducts |
| CN101073744A (en) * | 2006-09-13 | 2007-11-21 | 童裳慧 | Integrating apparatus fo magnesium oxide with desulfurizing, dust-collecting and energy-saving functions and its production |
| CN101530725A (en) * | 2009-03-11 | 2009-09-16 | 清华大学 | Flue gas desulfurization by magnesia wet method and recovering process of automatic concentration of product |
| CN101544437A (en) * | 2009-04-30 | 2009-09-30 | 河北工业大学 | Process method for recovering ammonium chloride and sodium chloride from waste water containing ammonium chloride and sodium chloride |
| CN205084611U (en) * | 2015-10-13 | 2016-03-16 | 日胜兴应用材料股份有限公司 | Magnesium method desulfurization zero release recovery system |
| CN206173242U (en) * | 2016-11-16 | 2017-05-17 | 山东旭霸生物科技有限公司 | Water -soluble fertilizer production system |
| CN107308662A (en) * | 2017-04-13 | 2017-11-03 | 北京浦仁美华环保科技股份有限公司 | The MVR evaporating, concentrating and crystallizing techniques of lithium are extracted from salt lake bittern |
| CN207102318U (en) * | 2017-07-14 | 2018-03-16 | 承德信通首承矿业有限责任公司 | Aoxidize magnesium liquid vapour vortex phase transformation integrated desulfurization device |
| CN108310935A (en) * | 2018-04-23 | 2018-07-24 | 焦作市雾神化工设备有限公司 | A kind of magnesium oxide method desulfurizing and drying all-in-one machine and construction method |
| CN208071367U (en) * | 2018-03-01 | 2018-11-09 | 中国电建集团透平科技有限公司 | A kind of MVR multi-effect evaporators for desulfurization wastewater processing |
-
2018
- 2018-11-16 CN CN201811364224.5A patent/CN109395552B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2665245A1 (en) * | 1990-07-27 | 1992-01-31 | Entropie Sa | Unit for concentrating a heat-sensitive solution, in particular grape must |
| JPH10109013A (en) * | 1996-10-04 | 1998-04-28 | Hisaji Koyama | Magnesium oxide and regenerated sulfuric acid recovering type flue gas desulfurization apparatus |
| US20040018133A1 (en) * | 2002-07-23 | 2004-01-29 | Radway Jerrold E. | Combustion emissions control and utilization of byproducts |
| CN101073744A (en) * | 2006-09-13 | 2007-11-21 | 童裳慧 | Integrating apparatus fo magnesium oxide with desulfurizing, dust-collecting and energy-saving functions and its production |
| CN101530725A (en) * | 2009-03-11 | 2009-09-16 | 清华大学 | Flue gas desulfurization by magnesia wet method and recovering process of automatic concentration of product |
| CN101544437A (en) * | 2009-04-30 | 2009-09-30 | 河北工业大学 | Process method for recovering ammonium chloride and sodium chloride from waste water containing ammonium chloride and sodium chloride |
| CN205084611U (en) * | 2015-10-13 | 2016-03-16 | 日胜兴应用材料股份有限公司 | Magnesium method desulfurization zero release recovery system |
| CN206173242U (en) * | 2016-11-16 | 2017-05-17 | 山东旭霸生物科技有限公司 | Water -soluble fertilizer production system |
| CN107308662A (en) * | 2017-04-13 | 2017-11-03 | 北京浦仁美华环保科技股份有限公司 | The MVR evaporating, concentrating and crystallizing techniques of lithium are extracted from salt lake bittern |
| CN207102318U (en) * | 2017-07-14 | 2018-03-16 | 承德信通首承矿业有限责任公司 | Aoxidize magnesium liquid vapour vortex phase transformation integrated desulfurization device |
| CN208071367U (en) * | 2018-03-01 | 2018-11-09 | 中国电建集团透平科技有限公司 | A kind of MVR multi-effect evaporators for desulfurization wastewater processing |
| CN108310935A (en) * | 2018-04-23 | 2018-07-24 | 焦作市雾神化工设备有限公司 | A kind of magnesium oxide method desulfurizing and drying all-in-one machine and construction method |
Non-Patent Citations (3)
| Title |
|---|
| 孙传尧: "《选矿工程师手册 第2册 上 选矿通论》", 31 March 2015, 冶金工业出版社 * |
| 戚长政主编: "《轻工自动机与生产线》", 31 July 2006, 中国轻工业出版社 * |
| 王泽廉: "《工业中化学》", 31 January 1988, 天津科学技术出版社 * |
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