CN108455775A - A kind of twin flue embrane method denitrification apparatus and application method - Google Patents
A kind of twin flue embrane method denitrification apparatus and application method Download PDFInfo
- Publication number
- CN108455775A CN108455775A CN201810357988.5A CN201810357988A CN108455775A CN 108455775 A CN108455775 A CN 108455775A CN 201810357988 A CN201810357988 A CN 201810357988A CN 108455775 A CN108455775 A CN 108455775A
- Authority
- CN
- China
- Prior art keywords
- embrane method
- caldo
- electrolytic cell
- nitre
- pipeline
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/22—Treatment of water, waste water, or sewage by freezing
-
- 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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
Abstract
The present invention relates to a kind of twin flue embrane method denitrification apparatus and application method, device to include：Salt dissolving dissolved salt unit（1）, storage tank（2）, primary purification refrigeration system and secondary refining cooling system.Preparation method includes the following steps：S1 salt dissolving dissolved salts：Pretreated light salt brine is sent in salt dissolving dissolved salt unit, saturation crude brine is prepared, saturation crude brine is delivered in crude salt water storage tank；S2 allotment refinings：In S1 steps 18 ~ 20% crude brine is delivered in electrolytic cell I, primary purification is carried out after former brine mixing preparation is added, storage tank A is delivered to after refined2In；S3 embrane methods remove nitre：Embrane method is delivered to except in nitre device, high caldo and low caldo is obtained by film feed pump after S2 steps are refined, high caldo is removed into nitre by freezing twice, sodium chloride crystal is precipitated, centrifugal filtration obtains sodium chloride crystal；S4 secondary refining embrane methods are recycled except nitre.The present invention has the advantages that at low cost, efficient and device is easy to operate.
Description
Technical field
The present invention relates to chlor-alkali production technology field, a kind of specific twin flue embrane method denitrification apparatus and application method.
Background technology
At present both at home and abroad there are many method of removing sulfate anion in brine system, and it is more commonly used have barium chloride method, freezing,
Calcium Chloride Method, embrane method denitration.All there is operating cost height, generation pollution environment to some extent for traditional chemical denitrating technique
Waste residue the problems such as, and in subtractive process addition to the harmful ion of ionic membrane.Embrane method denitration be substantially film concentration+it is cold
Freeze denitration, embrane method denitration technology is realized the separation of sulfate radical by physical method using macromolecule non-porous film, made in dense salt made from earth containing a comparatively high percentage of sodium chloride water
Sulfate radical content reaches 40g/l or so, then so that sulfate crystal is precipitated by freezing in dense salt made from earth containing a comparatively high percentage of sodium chloride water, by centrifuge from
Removing comes out in brine system.
Nitrate removal technology by membrane is Current Domestic, international technique the most perfect, and technical process is without using poisonous and hazardous
Refining agent is added to the harmful foreign ion of ionic membrane not into brine system, does not generate solid, liquid waste, operational management, behaviour
Make easy to maintain, saving production cost.Using freezing technique of nitrate removal, brine is after circulating frozen, through settling, centrifuging,
Sulfate radical is separated in the form of saltcake from brine, and low nitre halogen is saturated for brine section and refines, and saltcake is after evaporating, drying
By-product saltcake.
Freezing technique of nitrate removal causes freezing electric consumption high because needing a large amount of cold to freeze brine, year consumption freezing electricity at
About 15,000,000 yuan, hundred caustic soda of folding per ton freeze about 70 yuan of brine electric cost, after the chlor-alkali plant membrane system of in August, 2016 is shut down,
It being reduced with brine ratio, freezing electrolysis light salt brine amount increases, and hundred caustic soda of folding per ton freezing brine electric cost increases to about 115 yuan,
Production of caustic soda cost increases.
Invention content
It is an object of the invention to overcome the deficiencies of the prior art and provide a kind of twin flue embrane method denitrification apparatus and users
Method solves the problems, such as that common technique of nitrate removal power consumption is high, water consumption is big and of high cost.
The purpose of the present invention is achieved through the following technical solutions：
A kind of device of twin flue embrane method denitration, including：Salt dissolving dissolved salt unit, storage tank, primary purification refrigeration system and two
Secondary refined cooling system；
The storage tank：Storage tank is connected with salt dissolving dissolved salt unit by pipeline, further includes outlet I and outlet II on storage tank；
The primary purification cooling system includes：Electrolytic cell I, embrane method remove nitre device, freezing chamber and centrifuge；Electrolytic cell I
It is connected by pipeline with storage tank, and electrolytic cell I is connected with concentraing pond by pipeline；Embrane method passes through pipeline and electricity except nitre device
Solution slot I is connected, and it further includes high caldo outlet, the outlet of low caldo that embrane method, which is removed on nitre device,；Freezing chamber is with embrane method except nitre fills
It sets and is connected by pipeline；Centrifuge is connected by pipeline with freezing chamber；
The secondary refining cooling system includes：Electrolytic cell II, embrane method remove nitre device, freezing chamber and centrifuge；The electricity
Solution slot II is connected with storage tank by pipeline, and with embrane method except nitre device is connected by pipeline, electrolytic cell II is also wrapped electrolytic cell II
Include inlet and outlet；Freezing chamber is with embrane method except nitre device is connected by pipeline；Centrifuge passes through pipeline and freezing chamber phase
Connection.
Further, the outlet I is connected by pipeline with electrolytic cell I；The outlet II passes through pipeline and electrolytic cell
II is connected.
Further, the high caldo outlet is connected by pipeline with freezing chamber；The low caldo outlet passes through
Pipeline is connected with the water inlet of electrolytic cell II；The water outlet of the electrolytic cell II is with embrane method except the water inlet end of nitre device is connected
It is logical.
The application method of above-mentioned twin flue embrane method denitrification apparatus, includes the following steps：
S1 salt dissolving dissolved salts：Pretreated light salt brine is sent in salt dissolving dissolved salt unit, saturation crude brine is prepared, will satisfied
It is delivered in crude salt water storage tank with crude brine；
S2 allotment refinings：In S1 steps 18~20% crude brine is delivered in electrolytic cell I, is added in concentraing pond
Primary purification is carried out after former brine mixing preparation；
S3 embrane methods remove nitre：Embrane method is delivered to by film feed pump to remove in nitre device, obtain high caldo after S2 steps are refined
With low caldo, high caldo is passed through in the pipeline to freezing chamber of high caldo outlet connection and removed by freezing twice
Nitre, be precipitated sodium chloride crystal, in centrifuge centrifugal filtration obtain sodium chloride crystal；
S4 secondary refining embrane methods are recycled except nitre：Gone out by low caldo after the filtrate being obtained by filtration and low caldo are mixed
In the pipeline to electrolytic cell II of mouthful connection, then by S1 step residue crude brines be delivered in electrolytic cell II mixing carry out it is secondary
It is refined, embrane method is delivered to by film feed pump and is removed in nitre device, high caldo and low caldo is obtained, high caldo is passed through into height
Caldo outlet connection pipeline to freezing chamber in by twice freezing remove nitre, be precipitated sodium chloride crystal, in centrifuge from
Sodium chloride crystal is obtained by filtration in the heart.
Nitrate removal technology by membrane technical process does not use poisonous and hazardous refining agent, is added to ionic membrane not into brine system
Harmful foreign ion, does not generate solid, liquid waste, and operational management, convenient operating maintenance save production cost.It was preparing
Cheng Zhong carries out refined freezing using twin flue access, and the purity for the saltcake that freezing and crystallizing obtains is high, and impurity content is few, and yield
It is high；In existing embrane method except nitre device is immovable so that in the case of the same dense salt made from earth containing a comparatively high percentage of sodium chloride water of flow, corresponding precipitation is more
Sodium chloride crystal, improve embrane method remove nitre device production capacity, preferably ensure that the brine of qualified sodium sulphate index.It prepares
Method is simple, and operation is easier, and operability is stronger, and device operation is more steady efficient, the device utilization of capacity and load
Rate is compared with existing apparatus higher；Water consumption power consumption reduces in preparation process, reduces energy consumption, reduces cost；In preparation process not
Pollution auxiliary agent is added, it is environmentally friendly, also reduce cost.Twin flue embrane method technique of nitrate removal uses two sets of processing systems, the two
The saltcake of high-purity high-yield can be prepared in conjunction with production, process cycle can be also saved in preparation process, it also can will be low
Caldo recycles, and improves saltcake yield.
Further, pretreated light salt brine is in the S1 steps：It is free that sodium sulfite removal is added into light salt brine
For chlorine to zero, light salt brine is cooled to 10~20 DEG C by dechlorinated brine cooler, then adjusts pH to 6~7, and oxidation-reduction potential≤
100mV。
Further, the sulfate radical content of mixed liquor is 5.8~6.2g/L after being allocated in the S2 steps.
Further, the steam pressure that embrane method removes nitre device in the S3 steps is 0.4~0.6MPa, and pure water pressure is
0.4~0.6MPa, circulating water pressure be 0.4~0.5MPa, compressed air be 0.6~0.8MPa, instrument air be 0.6~
0.8MPa。
Further, sulfate radical content is 46.5~47.0g/L in high caldo in the S3 steps, sulphur in low caldo
Acid group content is 4.5~5.5g/L；Sulfate radical content is 46.5~47.0g/L in high caldo in the S4 steps.
Further, 10% sodium hydrate aqueous solution is added in the S2 steps in electrolytic cell I, adjusts pH to 10~11；
10% sodium hydrate aqueous solution is added in the S4 steps in electrolytic cell II, adjusts pH to 10~11.
Further, freezing is twice in the S3 steps：After freezing 45~60min at -10~-8 DEG C, continue -3~
0 DEG C of 80~100min of freezing；Freezing is twice in the S4 steps：After freezing 45~60min at -10~-8 DEG C, continue -3
~0 DEG C of 80~100min of freezing.
The beneficial effects of the invention are as follows：
1. Nitrate removal technology by membrane technical process does not use poisonous and hazardous refining agent, it is added to ion not into brine system
The harmful foreign ion of film, does not generate solid, liquid waste, and operational management, convenient operating maintenance save production cost；
2. in preparation process, refined freezing is carried out using twin flue access, the purity for the saltcake that freezing and crystallizing obtains is high,
Impurity content is few, and high income；Make the feelings of the same dense salt made from earth containing a comparatively high percentage of sodium chloride water of flow except nitre device is immovable in existing embrane method
Under condition, more sodium chloride crystals are accordingly precipitated, improves the production capacity that embrane method removes nitre device, preferably ensure that qualified sulfuric acid
The brine of sodium index；
3. preparation method is simple, operation is easier, and operability is stronger, and device operation is more steady efficient, dress
The utilization of capacity and rate of load condensate are set compared with existing apparatus higher；Water consumption power consumption reduces in preparation process, reduces energy consumption, reduces cost；
Do not add pollution auxiliary agent in preparation process, it is environmentally friendly, also reduce cost；It is efficient in preparation process, with routine
Being compared except nitre device has higher yield in unit time and working efficiency；
4. twin flue embrane method technique of nitrate removal uses two sets of processing systems, the two that high-purity height can be prepared in conjunction with production
The saltcake of yield can also save process cycle in preparation process, can also recycle low caldo, improve saltcake yield.
Description of the drawings
Fig. 1 is apparatus of the present invention schematic diagram；
In figure, 1- salt dissolving dissolved salt units, 2- storage tanks, the outlets the 21- outlet I, 22- II, 3- electrolytic cells I, 5- embrane method are except nitre dress
It sets, the outlet of 51- high caldos, the low caldo outlets 52-, 6- freezing chambers, 7- centrifuges, 8- concentraing ponds, 9- electrolytic cells II, 91-
Water inlet, 92- water outlets.
Specific implementation mode
Technical scheme of the present invention is described in further detail with reference to specific embodiment, but protection scope of the present invention is not
It is confined to as described below.
As shown in Figure 1, a kind of device of twin flue embrane method denitration, including：Salt dissolving dissolved salt unit 1, storage tank 2, primary purification
Refrigeration system and secondary refining cooling system；
The storage tank 2：Storage tank 2 is connected with salt dissolving dissolved salt unit 1 by pipeline, further includes outlet 21 Hes of I on storage tank 2
Export II 22；
The primary purification cooling system includes：Electrolytic cell I 3, embrane method remove nitre device 5, freezing chamber 6 and centrifuge 7；Electricity
Solution slot I 3 is connected with storage tank 2 by pipeline, and electrolytic cell I 3 is connected with concentraing pond 8 by pipeline；Embrane method removes nitre device 5
It is connected with electrolytic cell I 3 by pipeline, it further includes high caldo outlet 51, low caldo outlet 52 that embrane method, which is removed on nitre device 5,；
Freezing chamber 6 is with embrane method except nitre device 5 is connected by pipeline；Centrifuge 7 is connected by pipeline with freezing chamber 6；
The secondary refining cooling system includes：Electrolytic cell II 9, embrane method remove nitre device 5, freezing chamber 6 and centrifuge 7；Institute
Electrolytic cell II 9 is stated with storage tank 2 to be connected by pipeline, electrolytic cell II 9 with embrane method except nitre device 5 is connected by pipeline, electricity
It further includes water inlet 91 and water outlet 92 to solve slot II 9；Freezing chamber 6 is with embrane method except nitre device 5 is connected by pipeline；Centrifuge 7
It is connected with freezing chamber 6 by pipeline.
Specifically, the outlet I 21 is connected by pipeline with electrolytic cell I 3；The outlet II 22 by pipeline with
Electrolytic cell II 9 is connected.
Specifically, the high caldo outlet 51 is connected by pipeline with freezing chamber 6；The low caldo outlet 52 is logical
Piping is connected with the water inlet 91 of electrolytic cell II 9；The water outlet 92 of the electrolytic cell II 9 is with embrane method except nitre device 5
Water inlet end is connected.
Embodiment 1
The application method of twin flue embrane method denitrification apparatus, includes the following steps：
S1 salt dissolving dissolved salts：It pre-processes and sodium sulfite is added into light salt brine removes free chlorine to zero, dechlorinated brine-cooled
Light salt brine is cooled to 10 DEG C by device, then adjusts pH to 6, oxidation-reduction potential≤100mV, and pretreated light salt brine is sent to salt dissolving
Saturation crude brine is prepared in dissolved salt unit 1, saturation crude brine is delivered in crude salt water storage tank 2；
S2 allotment refinings：In S1 steps 18% crude brine is delivered in electrolytic cell I 3,10% sodium hydroxide water is added
Solution adjusts pH to 10, and the former brine mixing preparation added in concentraing pond 8 to sulfate radical content is 5.8g/L, carries out primary
It is refined；
S3 embrane methods remove nitre：Embrane method is delivered to by film feed pump to remove in nitre device 5, obtain high caldo after S2 steps are refined
With low caldo, high caldo is removed into nitre by freezing twice：80min precipitation awns is freezed at -3 DEG C after freezing 45min at -10 DEG C
Nitre crystallizes, and centrifugal filtration obtains sodium chloride crystal；
S4 secondary refining embrane methods are recycled except nitre：It is delivered to refinery pit II after the filtrate being obtained by filtration and low caldo are mixed
In, 10% sodium hydrate aqueous solution is added, adjusts pH to 10, then S1 step residue crude brines are delivered in electrolytic cell II 9 and are mixed
It closes and carries out secondary refining, being delivered to embrane method by film feed pump removes in nitre device 5, obtains high caldo and low caldo, will be high
Caldo removes nitre by freezing twice：80min precipitation sodium chloride crystals, centrifugation are freezed at -3~0 DEG C after freezing 45min at -10 DEG C
Sodium chloride crystal is obtained by filtration.
Specifically, the steam pressure that embrane method removes nitre device 5 in the S3 steps is 0.4~0.6MPa, and pure water pressure is 0.4
~0.6MPa, circulating water pressure are 0.4~0.5MPa, and compressed air is 0.6~0.8MPa, and instrument air is 0.6~0.8MPa；
The steam pressure that embrane method removes nitre device 5 in the S4 steps is 0.4~0.6MPa, and pure water pressure is 0.4~0.6MPa, recirculated water
Pressure is 0.4~0.5MPa, and compressed air is 0.6~0.8MPa, and instrument air is 0.6~0.8MPa.
Specifically, sulfate radical content is 46.5g/L in high caldo in the S3 steps, sulfate radical content in low caldo
For 4.5g/L；Sulfate radical content is 46.5g/L in high caldo in the S4 steps.
Other more existing devices of saltcake yield in unit time are high by about 12~15% in embodiment 1, while the device year utilization of capacity
Up to 92% or more, it is higher than other devices by about 25~35%.
Embodiment 2
The application method of twin flue embrane method denitrification apparatus, includes the following steps：
S1 salt dissolving dissolved salts：It pre-processes and sodium sulfite is added into light salt brine removes free chlorine to zero, dechlorinated brine-cooled
Light salt brine is cooled to 15 DEG C by device, then adjusts pH to 6.5, oxidation-reduction potential≤100mV, by pretreated sending to of light salt brine
Saturation crude brine is prepared in salt dissolved salt unit 1, saturation crude brine is delivered in crude salt water storage tank 2；
S2 allotment refinings：In S1 steps 19% crude brine is delivered in electrolytic cell I 3,10% sodium hydroxide water is added
Solution adjusts pH to 10.8, and the former brine mixing preparation added in concentraing pond 8 to sulfate radical content is 6.0g/L, carries out one
It is secondary refined；
S3 embrane methods remove nitre：Embrane method is delivered to by film feed pump to remove in nitre device 5, obtain high caldo after S2 steps are refined
With low caldo, high caldo is removed into nitre by freezing twice：90min precipitation awns is freezed at -2 DEG C after freezing 55min at -9 DEG C
Nitre crystallizes, and centrifugal filtration obtains sodium chloride crystal；
S4 secondary refining embrane methods are recycled except nitre：It is delivered to refinery pit II after the filtrate being obtained by filtration and low caldo are mixed
In, 10% sodium hydrate aqueous solution is added, pH is adjusted and is delivered in electrolytic cell II 9 to 10.8, then by S1 step residue crude brines
Mixing carries out secondary refining, and being delivered to embrane method by film feed pump removes in nitre device 5, obtains high caldo and low caldo, will
High caldo removes nitre by freezing twice：90min precipitation sodium chloride crystals are freezed at -2 DEG C after freezing 55min at -9 DEG C, are centrifuged
Filter obtains sodium chloride crystal.
Specifically, the steam pressure that embrane method removes nitre device 5 in the S3 steps is 0.4~0.6MPa, and pure water pressure is 0.4
~0.6MPa, circulating water pressure are 0.4~0.5MPa, and compressed air is 0.6~0.8MPa, and instrument air is 0.6~0.8MPa；
The steam pressure that embrane method removes nitre device 5 in the S4 steps is 0.4~0.6MPa, and pure water pressure is 0.4~0.6MPa, recirculated water
Pressure is 0.4~0.5MPa, and compressed air is 0.6~0.8MPa, and instrument air is 0.6~0.8MPa.
Specifically, sulfate radical content is 46.8g/L in high caldo in the S3 steps, sulfate radical content in low caldo
For 5.0g/L；Sulfate radical content is 46.8g/L in high caldo in the S4 steps.
Other more existing devices of saltcake yield in unit time are high by about 12~15% in embodiment 2, while the device year utilization of capacity
Up to 92% or more, it is higher than other devices by about 25~35%.
Embodiment 3
The application method of twin flue embrane method denitrification apparatus, includes the following steps：
S1 salt dissolving dissolved salts：It pre-processes and sodium sulfite is added into light salt brine removes free chlorine to zero, dechlorinated brine-cooled
Light salt brine is cooled to 20 DEG C by device, then adjusts pH to 7, oxidation-reduction potential≤100mV, and pretreated light salt brine is sent to salt dissolving
Saturation crude brine is prepared in dissolved salt unit 1, saturation crude brine is delivered in crude salt water storage tank 2；
S2 allotment refinings：In S1 steps 20% crude brine is delivered in electrolytic cell I 3,10% sodium hydroxide water is added
Solution adjusts pH to 11, and the former brine mixing preparation added in concentraing pond 8 to sulfate radical content is 6.2g/L, carries out primary
It is refined；
S3 embrane methods remove nitre：Embrane method is delivered to by film feed pump to remove in nitre device 5, obtain high caldo after S2 steps are refined
With low caldo, high caldo is removed into nitre by freezing twice：100min precipitation awns is freezed at 0 DEG C after freezing 60min at -8 DEG C
Nitre crystallizes, and centrifugal filtration obtains sodium chloride crystal；
S4 secondary refining embrane methods are recycled except nitre：It is delivered to refinery pit II after the filtrate being obtained by filtration and low caldo are mixed
In, 10% sodium hydrate aqueous solution is added, adjusts pH to 11, then S1 step residue crude brines are delivered in electrolytic cell II 9 and are mixed
It closes and carries out secondary refining, being delivered to embrane method by film feed pump removes in nitre device 5, obtains high caldo and low caldo, will be high
Caldo removes nitre by freezing twice：100min precipitation sodium chloride crystals, centrifugal filtration are freezed at 0 DEG C after freezing 60min at -8 DEG C
Obtain sodium chloride crystal.
Specifically, the steam pressure that embrane method removes nitre device 5 in the S3 steps is 0.4~0.6MPa, and pure water pressure is 0.4
~0.6MPa, circulating water pressure are 0.4~0.5MPa, and compressed air is 0.6~0.8MPa, and instrument air is 0.6~0.8MPa；
The steam pressure that embrane method removes nitre device 5 in the S4 steps is 0.4~0.6MPa, and pure water pressure is 0.4~0.6MPa, recirculated water
Pressure is 0.4~0.5MPa, and compressed air is 0.6~0.8MPa, and instrument air is 0.6~0.8MPa.
Specifically, sulfate radical content is 47.0g/L in high caldo in the S3 steps, sulfate radical content in low caldo
For 4.5~5.5g/L；Sulfate radical content is 47.0g/L in high caldo in the S4 steps.
Other more existing devices of saltcake yield in unit time are high by about 12~15% in embodiment 3, while the device year utilization of capacity
Up to 92% or more, it is higher than other devices by about 25~35%.
Embodiment 4
The application method of twin flue embrane method denitrification apparatus, includes the following steps：
S1 salt dissolving dissolved salts：It pre-processes and sodium sulfite is added into light salt brine removes free chlorine to zero, dechlorinated brine-cooled
Light salt brine is cooled to 18 DEG C by device, then adjusts pH to 6.5, oxidation-reduction potential≤100mV, by pretreated sending to of light salt brine
Saturation crude brine is prepared in salt dissolved salt unit 1, saturation crude brine is delivered in crude salt water storage tank 2；
S2 allotment refinings：In S1 steps 19% crude brine is delivered in electrolytic cell I 3,10% sodium hydroxide water is added
Solution adjusts pH to 10.4, and the former brine mixing preparation added in concentraing pond 8 to sulfate radical content is 5.9g/L, carries out one
It is secondary refined；
S3 embrane methods remove nitre：Embrane method is delivered to by film feed pump to remove in nitre device 5, obtain high caldo after S2 steps are refined
With low caldo, high caldo is removed into nitre by freezing twice：90min precipitation awns is freezed at -2 DEG C after freezing 55min at -9 DEG C
Nitre crystallizes, and centrifugal filtration obtains sodium chloride crystal；
S4 secondary refining embrane methods are recycled except nitre：It is delivered to refinery pit II after the filtrate being obtained by filtration and low caldo are mixed
In, 10% sodium hydrate aqueous solution is added, pH is adjusted and is delivered in electrolytic cell II 9 to 10.4, then by S1 step residue crude brines
Mixing carries out secondary refining, and being delivered to embrane method by film feed pump removes in nitre device 5, obtains high caldo and low caldo, will
High caldo removes nitre by freezing twice：90min precipitation sodium chloride crystals are freezed at -2 DEG C after freezing 55min at -9 DEG C, are centrifuged
Filter obtains sodium chloride crystal.
Specifically, the steam pressure that embrane method removes nitre device 5 in the S3 steps is 0.4~0.6MPa, and pure water pressure is 0.4
~0.6MPa, circulating water pressure are 0.4~0.5MPa, and compressed air is 0.6~0.8MPa, and instrument air is 0.6~0.8MPa；
The steam pressure that embrane method removes nitre device 5 in the S4 steps is 0.4~0.6MPa, and pure water pressure is 0.4~0.6MPa, recirculated water
Pressure is 0.4~0.5MPa, and compressed air is 0.6~0.8MPa, and instrument air is 0.6~0.8MPa.
Specifically, sulfate radical content is 46.7g/L in high caldo in the S3 steps, sulfate radical content in low caldo
For 5.2g/L；Sulfate radical content is 46.8g/L in high caldo in the S4 steps.
Other more existing devices of saltcake yield in unit time are high by about 12~15% in embodiment 4, while the device year utilization of capacity
Up to 92% or more, it is higher than other devices by about 25~35%.
The above is only a preferred embodiment of the present invention, it should be understood that the present invention is not limited to described herein
Form is not to be taken as excluding other embodiments, and can be used for other combinations, modifications, and environments, and can be at this
In the text contemplated scope, modifications can be made through the above teachings or related fields of technology or knowledge.And those skilled in the art institute into
Capable modifications and changes do not depart from the spirit and scope of the present invention, then all should be in the protection domain of appended claims of the present invention
It is interior.
Claims (10)
1. a kind of device of twin flue embrane method denitration, which is characterized in that including：Salt dissolving dissolved salt unit（1）, storage tank（2）, primary essence
Fine frozen system and secondary refining cooling system；
The storage tank（2）：Storage tank（2）With salt dissolving dissolved salt unit（1）It is connected by pipeline, storage tank（2）On further include outlet I
（21）With outlet II（22）；
The primary purification cooling system includes：Electrolytic cell I（3）, embrane method remove nitre device（5）, freezing chamber（6）And centrifuge
（7）；Electrolytic cell I（3）With storage tank（2）It is connected by pipeline, and electrolytic cell I（3）With concentraing pond（8）It is connected by pipeline
It is logical；Embrane method removes nitre device（5）Pass through pipeline and electrolytic cell I（3）It is connected, embrane method removes nitre device（5）On further include high caldo
Outlet（51）, the outlet of low caldo（52）；Freezing chamber（6）Nitre device is removed with embrane method（5）It is connected by pipeline；Centrifuge（7）
Pass through pipeline and freezing chamber（6）It is connected；
The secondary refining cooling system includes：Electrolytic cell II（9）, embrane method remove nitre device（5）, freezing chamber（6）And centrifuge
（7）；The electrolytic cell II（9）With storage tank（2）It is connected by pipeline, electrolytic cell II（9）Nitre device is removed with embrane method（5）Pass through
Pipeline is connected, electrolytic cell II（9）It further include water inlet（91）And water outlet（92）；Freezing chamber（6）Nitre device is removed with embrane method
（5）It is connected by pipeline；Centrifuge（7）Pass through pipeline and freezing chamber（6）It is connected.
2. a kind of device of twin flue embrane method denitration according to claim 1, which is characterized in that the outlet I（21）It is logical
Piping and electrolytic cell I（3）It is connected；The outlet II（22）Pass through pipeline and electrolytic cell II（9）It is connected.
3. a kind of device of twin flue embrane method denitration according to claim 1, which is characterized in that the high caldo outlet
（51）Pass through pipeline and freezing chamber（6）It is connected；The low caldo outlet（52）Pass through pipeline and electrolytic cell II（9）Into
The mouth of a river（91）It is connected；The electrolytic cell II（9）Water outlet（92）Nitre device is removed with embrane method（5）Water inlet end be connected.
4. the application method of above-mentioned twin flue embrane method denitrification apparatus, which is characterized in that include the following steps：
S1 salt dissolving dissolved salts：Pretreated light salt brine is sent into salt dissolving dissolved salt unit（1）In saturation crude brine is prepared, will be saturated
Crude brine is delivered to crude salt water storage tank（2）In；
S2 allotment refinings：In S1 steps 18 ~ 20% crude brine is delivered to electrolytic cell I（3）In, add concentraing pond（8）In
Former brine mixing preparation after carry out primary purification；
S3 embrane methods remove nitre：Embrane method is delivered to by film feed pump after S2 steps are refined and removes nitre device（5）In, obtain high caldo and
Low caldo exports high caldo by high caldo（51）The pipeline of connection is to freezing chamber（6）Middle process is cold twice
Freeze and remove nitre, sodium chloride crystal is precipitated, in centrifuge（7）Middle centrifugal filtration obtains sodium chloride crystal；
S4 secondary refining embrane methods are recycled except nitre：It is exported by low caldo after the filtrate being obtained by filtration and low caldo are mixed
（52）The pipeline of connection is to electrolytic cell II（9）In, then S1 step residue crude brines are delivered to electrolytic cell II（9）In mix
It closes and carries out secondary refining, being delivered to embrane method by film feed pump removes nitre device（5）In, high caldo and low caldo are obtained, it will
High caldo is exported by high caldo（51）The pipeline of connection is to freezing chamber（6）It is middle to remove nitre by freezing twice, it is precipitated
Sodium chloride crystal, in centrifuge（7）Middle centrifugal filtration obtains sodium chloride crystal.
5. the application method of twin flue embrane method denitrification apparatus according to claim 4, which is characterized in that in the S1 steps
Pretreated light salt brine is：Sodium sulfite is added into light salt brine and removes free chlorine to zero, dechlorinated brine cooler is by light salt
10 ~ 20 DEG C are water-cooled to, then adjusts pH to 6 ~ 7, oxidation-reduction potential≤100mV.
6. the application method of twin flue embrane method denitrification apparatus according to claim 4, which is characterized in that in the S2 steps
The sulfate radical content of mixed liquor is 5.8 ~ 6.2g/L after allotment.
7. the application method of twin flue embrane method denitrification apparatus according to claim 4, which is characterized in that in the S3 steps
Embrane method except nitre device steam pressure be 0.4 ~ 0.6MPa, pure water pressure be 0.4 ~ 0.6MPa, circulating water pressure be 0.4 ~
0.5MPa, compressed air are 0.6 ~ 0.8MPa, and instrument air is 0.6 ~ 0.8MPa；Embrane method removes the steaming of nitre device in the S4 steps
Steam pressure be 0.4 ~ 0.6MPa, pure water pressure be 0.4 ~ 0.6MPa, circulating water pressure be 0.4 ~ 0.5MPa, compressed air be 0.6 ~
0.8MPa, instrument air are 0.6 ~ 0.8MPa.
8. the application method of twin flue embrane method denitrification apparatus according to claim 4, which is characterized in that in the S3 steps
Sulfate radical content is 46.5 ~ 47.0g/L in high caldo, and sulfate radical content is 4.5 ~ 5.5g/L in low caldo；The S4 steps
Sulfate radical content is 46.5 ~ 47.0g/L in high caldo in rapid.
9. the application method of twin flue embrane method denitrification apparatus according to claim 4, which is characterized in that in the S2 steps
10% sodium hydrate aqueous solution is added in electrolytic cell I, adjusts pH to 10 ~ 11；In the S4 steps 10% is added in electrolytic cell II
Sodium hydrate aqueous solution adjusts pH to 10 ~ 11.
10. the application method of twin flue embrane method denitrification apparatus according to claim 4, which is characterized in that the S3 steps
In twice freezing be：After freezing 45 ~ 60min at -10 ~ -8 DEG C, continue to freeze 80 ~ 100min at -3 ~ 0 DEG C；In the S4 steps
It freezes twice and is：After freezing 45 ~ 60min at -10 ~ -8 DEG C, continue to freeze 80 ~ 100min at -3 ~ 0 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810357988.5A CN108455775A (en) | 2018-04-20 | 2018-04-20 | A kind of twin flue embrane method denitrification apparatus and application method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810357988.5A CN108455775A (en) | 2018-04-20 | 2018-04-20 | A kind of twin flue embrane method denitrification apparatus and application method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108455775A true CN108455775A (en) | 2018-08-28 |
Family
ID=63236063
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810357988.5A Pending CN108455775A (en) | 2018-04-20 | 2018-04-20 | A kind of twin flue embrane method denitrification apparatus and application method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108455775A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117146483A (en) * | 2023-09-06 | 2023-12-01 | 内蒙古伊东集团东兴化工有限责任公司 | Heat exchange device and heat exchange method of denitration refrigerating unit by substituted membrane method |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007262443A (en) * | 2006-03-27 | 2007-10-11 | Nippon Rensui Co Ltd | Sodium chloride electrolisis method |
| CN101235510A (en) * | 2007-11-08 | 2008-08-06 | 山东海化氯碱树脂有限公司 | Method for removing SO4(2-) ion in ionic film electrolysis sodium hydroxide light salt water |
| CN102417193A (en) * | 2011-10-11 | 2012-04-18 | 山东东岳氟硅材料有限公司 | Production method for increasing nitrate removal capacity by membrane method |
| CN204174288U (en) * | 2014-09-26 | 2015-02-25 | 江苏理文化工有限公司 | A kind of ion film caustic soda production equipment improving bittern usage ratio |
| CN204752229U (en) * | 2015-07-01 | 2015-11-11 | 中盐金坛盐化有限责任公司 | System for be used for light salt solution to convert steamed denitration |
| CN106906485A (en) * | 2017-03-31 | 2017-06-30 | 四川永祥股份有限公司 | A kind of total Halogenated Caustic Production |
| CN107022770A (en) * | 2017-04-28 | 2017-08-08 | 湖北可赛化工有限公司 | The process system and method for a kind of high caldo perhalogeno ionic membrane alkaline |
| CN208829465U (en) * | 2018-04-20 | 2019-05-07 | 江苏安邦电化有限公司 | A kind of device of twin flue embrane method denitration |
-
2018
- 2018-04-20 CN CN201810357988.5A patent/CN108455775A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007262443A (en) * | 2006-03-27 | 2007-10-11 | Nippon Rensui Co Ltd | Sodium chloride electrolisis method |
| CN101235510A (en) * | 2007-11-08 | 2008-08-06 | 山东海化氯碱树脂有限公司 | Method for removing SO4(2-) ion in ionic film electrolysis sodium hydroxide light salt water |
| CN102417193A (en) * | 2011-10-11 | 2012-04-18 | 山东东岳氟硅材料有限公司 | Production method for increasing nitrate removal capacity by membrane method |
| CN204174288U (en) * | 2014-09-26 | 2015-02-25 | 江苏理文化工有限公司 | A kind of ion film caustic soda production equipment improving bittern usage ratio |
| CN204752229U (en) * | 2015-07-01 | 2015-11-11 | 中盐金坛盐化有限责任公司 | System for be used for light salt solution to convert steamed denitration |
| CN106906485A (en) * | 2017-03-31 | 2017-06-30 | 四川永祥股份有限公司 | A kind of total Halogenated Caustic Production |
| CN107022770A (en) * | 2017-04-28 | 2017-08-08 | 湖北可赛化工有限公司 | The process system and method for a kind of high caldo perhalogeno ionic membrane alkaline |
| CN208829465U (en) * | 2018-04-20 | 2019-05-07 | 江苏安邦电化有限公司 | A kind of device of twin flue embrane method denitration |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117146483A (en) * | 2023-09-06 | 2023-12-01 | 内蒙古伊东集团东兴化工有限责任公司 | Heat exchange device and heat exchange method of denitration refrigerating unit by substituted membrane method |
| CN117146483B (en) * | 2023-09-06 | 2024-03-26 | 内蒙古伊东集团东兴化工有限责任公司 | Heat exchange device and heat exchange method of denitration refrigerating unit by substituted membrane method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2020147224A1 (en) | Method and system for preparing battery-grade, high-purity-grade lithium hydroxide and lithium carbonate from high-impurity lithium source | |
| CN105540619B (en) | Method for directly preparing battery grade lithium carbonate from salt lake brine with high magnesium-to-lithium ratio | |
| CN108341420B (en) | Method for directly preparing lithium hydroxide and lithium carbonate from salt lake brine with high magnesium-lithium ratio | |
| CN110065958B (en) | Method for preparing lithium hydroxide by treating salt lake brine through integrated selective electrodialysis and selective bipolar membrane electrodialysis | |
| CN102417193B (en) | Production method for increasing nitrate removal capacity by membrane method | |
| CN111960445A (en) | Method for preparing battery-grade lithium carbonate by using lithium sulfate coarse ore and recycling by-products | |
| CN210736624U (en) | Production system for recycling taurine mother liquor completely | |
| CN102092880B (en) | Process for freezing and denitriding primary brine with membrane method in polyvinyl chloride production | |
| CN108455775A (en) | A kind of twin flue embrane method denitrification apparatus and application method | |
| CN208829465U (en) | A kind of device of twin flue embrane method denitration | |
| CN104150519B (en) | A kind of method utilizing sodium sulfate waste liquid to prepare barium sulfate and sodium carbonate | |
| CN217051939U (en) | Sulfate radical desorption system in potash light brine | |
| CN205933261U (en) | Lithium hydroxide's purification and separation system | |
| WO2023168896A1 (en) | Bipolar membrane system for efficiently removing magnesium ions in salt lake brine by means of in-situ alkali production | |
| CA1313161C (en) | Process for the production of alkali metal chlorate | |
| CN205328787U (en) | Zinc borate waste water's resourceful treatment system | |
| CN203683295U (en) | Denitration system of light salt brine by membrane method | |
| CN109809582A (en) | A kind of potassium sulfate Sewage treatment utilizes method | |
| CN109748310A (en) | A kind of separation method of barium sulfate and potassium carbonate mixed solution | |
| CN110723857B (en) | High-salinity water concentration and crystallization treatment system and process | |
| CN211111482U (en) | Lithium carbonate washing water resource comprehensive utilization's device | |
| RU91530U1 (en) | PLANT FOR PRODUCING CAUSTIC SODA FROM ELECTROLYTIC ALKALI | |
| CN219209534U (en) | Production system for preparing lithium hydroxide by taking lithium carbonate as raw material | |
| CN219792515U (en) | Green co-production device of battery level sodium carbonate and fused salt level sodium nitrate | |
| CN211896069U (en) | System for continuously producing electroplating-grade copper oxide by using circuit board etching waste liquid as raw material |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |