CN206736369U - A kind of process system of high caldo perhalogeno ionic membrane alkaline - Google Patents
A kind of process system of high caldo perhalogeno ionic membrane alkaline Download PDFInfo
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- CN206736369U CN206736369U CN201720462293.4U CN201720462293U CN206736369U CN 206736369 U CN206736369 U CN 206736369U CN 201720462293 U CN201720462293 U CN 201720462293U CN 206736369 U CN206736369 U CN 206736369U
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Abstract
The utility model belongs to industrial alkali making technology field, and in particular to a kind of process system of high caldo perhalogeno ionic membrane alkaline.The system includes adopting in the high caldo pipeline of halogen conveying, TOC adsorption subsystems, the organic tubular membrane filter subsystem of normal temperature, nanofiltration subsystem, freezing denitration subsystem, deamination and subsystem, secondary refining electrolysis subsystem and light salt brine return well casing road.The utility model can refine denitration to high caldo, refined brine be directly obtained, for ionic membrane alkaline.
Description
Technical field
The utility model belongs to industrial alkali making technology field, and in particular to a kind of work of high caldo perhalogeno ionic membrane alkaline
Process system.
Background technology
The technology that existing high caldo alkaline enterprise uses has three kinds：One kind is total Halogenated Caustic Production, but bittern takes off
Nitre is using full freezing denitration technology, and non-embrane method denitration technology, investment is larger, and operating cost is high；The method difference that other two uses
It is：The first is that salt technique is mixed in light salt brine embrane method denitration, and crude salt consuming cost is high；Second is that light salt brine embrane method denitration adds light salt
Water concentration technology, investment is big, and running cost is higher.
The Chinese patent of Application No. 201110185103.6 discloses a kind of method of total halogenated caustic production, by light salt brine
Except free chlorine, except inferior sulfate radical and sulfate radical and evaporation and concentration, resin treatment obtain secondary brine, reach light salt brine recovery
Purpose.Generally, its high energy consumption, investment is big, and has the consumption of additive.
It is overall, the current embrane method denitration technology for having 200g/L and 250g/L salt solution, saturated brine (NaCl contents >=
300g/L) receive film denitration (SO4 2-) in technology industry also without using precedent.
Utility model content
To solve the deficiencies in the prior art, the utility model provides a kind of technique of high caldo perhalogeno ionic membrane alkaline
System.Technical scheme provided by the utility model is to realize the new technology of total halogenated caustic production using embrane method denitration to high caldo,
It can realize that the high caldo of saturated brine carries out perhalogeno ionic membrane alkaline, reach live lean degree height, operating cost is most
Economy, crude salt is not consumed, reduce the effect of cost.
Technical scheme provided by the utility model is as follows：
A kind of process system of high caldo perhalogeno ionic membrane alkaline, including adopt the high caldo pipeline of halogen conveying, TOC suctions
In the organic tubular membrane filter subsystem of monkshood system, normal temperature, nanofiltration subsystem, freezing denitration subsystem, deamination and subsystem, two
Secondary refined electrolysis subsystem and light salt brine return well casing road, and the high caldo pipeline for adopting halogen conveying connects TOC absorption
System, the TOC adsorption subsystems connect the organic tubular membrane filter subsystem of normal temperature, the organic tubular type membrane filtration of normal temperature
Subsystem connects respectively in the nanofiltration subsystem and the deamination and subsystem, the nanofiltration subsystem connect described cold respectively
Freeze in denitration subsystem and the deamination and subsystem, the jelly denitration subsystem connect the nanofiltration subsystem by return pipe,
The secondary refining electrolysis subsystem is connected in the deamination with subsystem, the secondary refining electrolysis subsystem connection is described light
Salt solution returns well casing road.
The organic tubular membrane filter subsystem of normal temperature connects the nanofiltration subsystem and described by distribution pipeline respectively
In deamination and subsystem, the flow-rate ratio of two pipelines of distribution pipeline is 0.8~1.2:1.2~0.8, preferably 1:1.
The nanofiltration subsystem includes film leading portion and film back segment, the film front end connection freezing denitration subsystem, institute
Film back segment is stated to connect in the deamination and subsystem.
Pass through above-mentioned technical proposal, by a small amount of high nitre concentrate (10m after nanofiltration3/ h) freezing denitration is carried out, by denitration
Brine recycling utilizes, and to reduce production halogen amount, reduces the bittern usage amount of unit product, halogen is adopted in reduction and the electric energy of halogen transportation disappears
Consumption.
The light salt brine returns the connection of well casing road and removes salt well, can be used for adopting halogen afterwards.
Pass through above-mentioned technical proposal, can be by the light salt brine (45m after electrolysis3/ h) salt well re-injection is delivered to, solve light salt brine
Problem of outlet, to ensure total halogenated caustic production, and eliminate TOC (and Si, chlorate) and build up in systems.
The process system of the high caldo perhalogeno ionic membrane alkaline also includes at washing device, nano filter membrance device and neutralization
Device is managed, the washing device connects the TOC adsorption subsystems, and the TOC adsorption subsystems connect the nano filter membrance device,
The nano filter membrance device connects the neutralisation treatment device and connects the TOC adsorption subsystems, neutralisation treatment dress by return pipe
Old well can be reconnected by pipeline by putting.
Pass through above-mentioned technical proposal, it is miscellaneous to the deliming of high caldo progress normal temperature, magnesium with the organic tubular type membrane filtration system of normal temperature
Matter, it can not only ensure 60m3/ h salt refinings are needed, and technology has been lifted, and advantage protrudes：First, it can carry out at normal temperatures
Ultrafiltration is run, and the steam saving energy, second, being not required to carry out recoil operation, process is simple and direct, stable, efficiency high.
Can be to high caldo by the process system of high caldo perhalogeno ionic membrane alkaline provided by the utility model
Refined embrane method denitration is carried out, so as to obtain denitration refined brine, for production of ion-exchange-membrane caustic soda.
The utility model is based on " saturated brine receive membrane filtration denitration technology ", " removing calcium and magnesium is removed in the organic tubular membrane ultrafiltration of normal temperature
Technology " and " resin adsorption remove three big technologies of TOC " fusion, ionic membrane can be mixed stew in soy sauce alkali technological transformation for high caldo it is complete
Halogen ion film alkali-making process, then the denitration of light salt brine embrane method need not be carried out and mix the operation of salt weight saturation, light salt brine can direct re-injection
Salt well salt dissolving, production procedure greatly shorten；It is important that being not required to the solid salt of outsourcing, the cost of raw material is greatly reduced.By this reality
With the process system of new provided high caldo perhalogeno ionic membrane alkaline, refined embrane method can be carried out to high caldo and is taken off
Nitre, refined brine is directly obtained, for production of ion-exchange-membrane caustic soda.
Brief description of the drawings
Fig. 1 is the system diagram of the process system of high caldo perhalogeno ionic membrane alkaline provided by the utility model.
Fig. 2 is 50,000 tons/year of perhalogenos of the process system of high caldo perhalogeno ionic membrane alkaline provided by the utility model
Ionic membrane alkaline material balance schematic diagram.
In accompanying drawing 1, the structure list representated by each label is as follows：
1st, the high caldo pipeline of halogen conveying is adopted, 2, TOC adsorption subsystems, 3, the organic tubular membrane filter subsystem of normal temperature,
4th, nanofiltration subsystem, 5, freezing denitration subsystem, 6, in deamination and subsystem, 7, secondary refining electrolysis subsystem, 8, light salt brine
Return well casing road, 9, washing device, 10, nano filter membrance device, 11, neutralisation treatment device.
Embodiment
Principle of the present utility model and feature are described below, illustrated embodiment is served only for explaining the utility model,
It is not intended to limit the scope of the utility model.
In a detailed embodiment, as shown in figure 1, the process system of high caldo perhalogeno ionic membrane alkaline includes adopting
It is the high caldo pipeline 1 of halogen conveying, TOC adsorption subsystems 2, the organic tubular membrane filter subsystem 3 of normal temperature, nanofiltration subsystem 4, cold
Freeze in denitration subsystem 5, deamination and subsystem 6, secondary refining electrolysis subsystem 7, light salt brine return well casing road 8, washing device 9,
Nano filter membrance device 10 and neutralisation treatment device 11.
Enter high caldo pipeline 1 and connect TOC adsorption subsystems 2, TOC adsorption subsystems 2 connect the organic tubular membrane mistake of normal temperature
Filter system 3, the organic tubular membrane filter subsystem 3 of normal temperature connects nanofiltration subsystem 4 by distribution pipeline respectively and deamination neutralizes
Subsystem 6, the flow-rate ratio of two pipelines of distribution pipeline is 1：1.
Nanofiltration subsystem 4 includes film leading portion and film back segment, and film front end connection freezing denitration subsystem 5, the connection of film back segment is de-
Freeze denitration subsystem with subsystem 6 in ammonia and nanofiltration subsystem 4 is connected by return pipe, refined in deamination with the connecting secondary of subsystem 6
Subsystem 7 is electrolysed, secondary refining electrolysis subsystem 7 connects light salt brine and returns well casing road 8, and salt well is removed in the connection of light salt brine pipeline 8.
Washing device 9 connects TOC adsorption subsystems 2, and TOC adsorption subsystems 2 connect nano filter membrance device 10, nano filter membrance device
10 connection neutralisation treatment devices 11 simultaneously connect TOC adsorption subsystems 2 by return pipe.
Embodiment
Film alkaline is carried out with the process system of high caldo perhalogeno ionic membrane alkaline, comprised the following steps：
1) TOC absorption is carried out to high caldo, TOC absorption is carried out to high caldo with TOC adsorption systems, high caldo enters
The concentration of the salt of water is 270~305g/L；
2) normal temperature is carried out to high caldo to the high caldo by TOC absorption with the organic tubular type membrane filtration system of normal temperature to remove
Impurity, impurity are mainly calcium, magnesium ion；
3) the high salt made from earth containing a comparatively high percentage of sodium chloride moisture two-way by normal temperature deliming, magnesium addition, the high salt made from earth containing a comparatively high percentage of sodium chloride water of the first via are obtained by nanofiltration denitration
To low salt made from earth containing a comparatively high percentage of sodium chloride water, the high salt made from earth containing a comparatively high percentage of sodium chloride water in the second tunnel treats that deamination neutralizes, by liquid before the film of the high nitre obtained by nanofiltration denitration by freezing
Obtain freezing denitration salt solution after denitration, then freezing denitration salt solution is subjected to nanofiltration denitration, the high salt made from earth containing a comparatively high percentage of sodium chloride water of the first via and freezing denitration
Salt solution together enters nanofiltration denitrating system and carries out nanofiltration denitration, and the flow-rate ratio of the high salt made from earth containing a comparatively high percentage of sodium chloride water of the first via and the high salt made from earth containing a comparatively high percentage of sodium chloride water in the second tunnel is
1：1；
4) by low salt made from earth containing a comparatively high percentage of sodium chloride water with treating that the high salt made from earth containing a comparatively high percentage of sodium chloride water that deamination neutralizes mixes and carries out deamination neutralization；
5) by the refined brine neutralized by deamination through secondary refining, electrolysis with ion-exchange film.Generation light salt brine returns well.
As shown in Fig. 2 operation principle is as follows：
1) bittern is input to TOC adsorption towers first and removes system, TOC contents is touched the mark requirement ,≤
30mg/L；
2) organic tubular type membrane filtration (ultrafiltration) system of normal temperature is configured after TOC adsorption systems, after filtering out intermediate reaction
Mg(OH)2、CaCO3Deng impurity, it can not only ensure 60m3/ h salt refinings need, and are that can carry out ultrafiltration at normal temperatures
Operation, the steam saving energy, is not required to carry out recoil operation, process is simple and direct, stable, efficiency high；
3) with membrane filtration (nanofiltration) system is accommodated after ultrafiltration system, to filter out SO4 2-Ion：
Nanofiltration technique device can be by SO in saturated brine4 2-Content is removed to 2g/L by 12g/L, and electrolysis with ion-exchange film requires
≤ 8g/L, in order to which technological requirement should be met, mitigate receive film device load again, part salt is formulated as to the unit link
Water nanofiltration technique, i.e.,：
First, supermembrane filtered brine (NaCl=300g/L) is divided into two parts：
A part：I.e. wherein half (30m3/ h) and a small amount of denitration salt solution (10m3/ h) after mixing, squeeze into and receive membrane filtration system
(NF).Nanofiltration is carried out through nanofiltration system, 75% passes through filtering layer, SO4 2-Content drops to 2g/L, is " low salt made from earth containing a comparatively high percentage of sodium chloride water "；And 25% it is dense
Contracting liquid, SO4 2-Content is up to 42g/L, is " high salt made from earth containing a comparatively high percentage of sodium chloride water "；
Another part：That is second half (30m3/ h) low salt made from earth containing a comparatively high percentage of sodium chloride water (30m after salt solution without nanofiltration and nanofiltration3/ h) mixing,
It is formulated as SO4 2-Content 7g/L primary brine, neutralized, after secondary refining through deamination, electrolysis uses；
Secondly, by a small amount of high salt made from earth containing a comparatively high percentage of sodium chloride water (concentrate SO after above-mentioned nanofiltration4 2-Content about 42g/L), carry out denitration process；
Denitration salt solution (10m3/ h, SO4 2-Content about 10g/L) return again to nanofiltration system and carry out refined use；
After deamination neutralizes, NaCl >=300g/L, SO4 2-≤7g/L。
4) by the light salt brine (45m after electrolysis3/ h) salt well re-injection is delivered to, solve the problem of outlet of light salt brine, to ensure
Total halogenated caustic production, and eliminate TOC (and Si, chlorate) and build up in systems；
5) by a small amount of high nitre concentrate (10m after nanofiltration3/ h) freezing denitration is carried out, denitration brine recycling is utilized, with
Production halogen amount is reduced, reduces the bittern usage amount of unit product, halogen and the power consumption of halogen transportation are adopted in reduction.
Preferred embodiment of the present utility model is the foregoing is only, it is all in this practicality not to limit the utility model
Within new spirit and principle, any modification, equivalent substitution and improvements made etc., guarantor of the present utility model should be included in
Within the scope of shield.
Claims (5)
- A kind of 1. process system of high caldo perhalogeno ionic membrane alkaline, it is characterised in that：High caldo including adopting halogen conveying The organic tubular membrane filter subsystem (3) of pipeline (1), TOC adsorption subsystems (2), normal temperature, nanofiltration subsystem (4), freezing denitration In system (5), deamination and subsystem (6), secondary refining electrolysis subsystem (7) and light salt brine return well pipe-line system (8), described to adopt The high caldo pipeline (1) of halogen conveying connects the TOC adsorption subsystems (2), described in TOC adsorption subsystems (2) connection The organic tubular membrane filter subsystem (3) of normal temperature, the organic tubular membrane filter subsystem (3) of normal temperature connect nanofiltration respectively In system (4) and the deamination and subsystem (6), the nanofiltration subsystem (4) connect the freezing denitration subsystem (5) respectively With in the deamination and subsystem (6), the jelly denitration subsystem (5) connects the nanofiltration subsystem (4) by return pipe, described In deamination and subsystem (6) connects the secondary refining electrolysis subsystem (7), secondary refining electrolysis subsystem (7) connection The light salt brine returns well casing road (8).
- 2. the process system of high caldo perhalogeno ionic membrane alkaline according to claim 1, it is characterised in that：The normal temperature Organic tubular membrane filter subsystem (3) is connected respectively by distribution pipeline in the nanofiltration subsystem (4) and the deamination and son System (6).
- 3. the process system of high caldo perhalogeno ionic membrane alkaline according to claim 1, it is characterised in that：The nanofiltration Subsystem (4) includes film leading portion and film back segment, the film front end connection freezing denitration subsystem (5), and the film back segment connects Connect in the deamination and subsystem (6).
- 4. the process system of high caldo perhalogeno ionic membrane alkaline according to claim 1, it is characterised in that：The light salt Water returns well casing road (8) connection and removes salt well.
- 5. the process system of high caldo perhalogeno ionic membrane alkaline according to claim 1, it is characterised in that：The high nitre The process system of bittern perhalogeno ionic membrane alkaline also includes washing device (9), nano filter membrance device (10) and neutralisation treatment device (11), the washing device (9) connects the TOC adsorption subsystems (2), and the TOC adsorption subsystems (2) connect the nanofiltration Film device (10), the nano filter membrance device (10), which connects the neutralisation treatment device (11) and connects the TOC by return pipe, inhales Monkshood system (2).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720462293.4U CN206736369U (en) | 2017-04-28 | 2017-04-28 | A kind of process system of high caldo perhalogeno ionic membrane alkaline |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720462293.4U CN206736369U (en) | 2017-04-28 | 2017-04-28 | A kind of process system of high caldo perhalogeno ionic membrane alkaline |
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| CN206736369U true CN206736369U (en) | 2017-12-12 |
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| CN201720462293.4U Withdrawn - After Issue CN206736369U (en) | 2017-04-28 | 2017-04-28 | A kind of process system of high caldo perhalogeno ionic membrane alkaline |
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2017
- 2017-04-28 CN CN201720462293.4U patent/CN206736369U/en not_active Withdrawn - After Issue
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20171212 Effective date of abandoning: 20190426 |