When solid waste is generated, the potential for its disposal can be considered. Salts (NaCl, CaCl2, HCl and gypsum) can be disposed of, for example. These products can be obtained by evaporation or recrystallization of salt from flue gas cleaning system wastewater, either on site or in a centralized evaporation plant.
When scrubber effluents are treated separately and subjected to evaporation, recyclable products such as salts or hydrochloric acid can be obtained.
The recycling potential of such products is highly dependent on the quality of the product. In salt disposal, the scrubber effluents are treated with sodium hydroxide and calcium carbonate to produce hard gypsum, which after separation leaves a liquid containing mainly sodium and calcium chloride. The recycled product is subjected to quality control or even additional processing to improve quality, and then sold.
Achievable positive effect. The main purpose of the operation is to prevent the discharge of saline sewage into the sewerage system. This is achieved by evaporating the scrubber effluents from the flue gas cleaning system. If solid sodium chloride is to be separated individually from said solution, this is achieved by evaporating the solution to a salt content of more than 30%, at which level the pure salt crystallizes.
These recycled salt products are most frequently reused in regions for winter de-icing. Reusing saline salts can save natural resources.
Environmental impact. The main disadvantage of external wastewater evaporation for salts is not only operational and material problems, but also the high energy consumption required for evaporation.
operational features. Evaporation of wastewater containing salts depends on salt concentrations, which can vary greatly. In addition to corrosion problems, relatively high investment and operating costs must be taken into account.
For the production of gypsum alone, there are several operational problems. However, the quality of a gypsum is determined not only by its purity in relation to the presence of other undesirable components, but also by its color. Generally, production of recyclable products in the amount of about 2-5 kg per tonne of waste can be expected.
In the production of calcium chloride, emphasis must be placed on the possibility of excessive corrosion that may occur and on unintended phase transition from solid to liquid and vice versa.
Often, novice entrepreneurs, thinking about which business to open, do not pay any attention to seemingly completely obvious industries, in particular, the processing of minerals, etc.
At the same time, many are victims of the stereotype that the development and processing of minerals is the prerogative of state enterprises or large corporations. But this is far from true. Although large organizations, and even more so the state, of course, have more financial, administrative and other opportunities to develop deposits, some minerals, and in particular table salt, can be mined by small enterprises.
And even if it is not possible to engage in the extraction of salt, then the processing and subsequent sale is quite within the power of a novice businessman.
The only limitation of the table salt business is geographical. As you know, most of the salt deposits in Russia are located in the Volga region, respectively, and the enterprise should be opened there - this will help to avoid unnecessary transportation costs: salt, as you know, is the cheapest (after water) food additive, so any overexpenditure included in its the cost may at some point make it unprofitable.
In fact, the salt market is extremely sensitive to any price fluctuations, for example, for gasoline or electricity: by and large, the price of salt is the sum of the costs of its extraction and packaging, and the cost of raw materials can be considered zero (there are no material costs as such, there are only the cost of mining halite - a mineral of rock salt).
In addition to the development of halite deposits, it is sometimes practiced alternative way salt production - evaporation from salt water, for example, sea water, or water from saline or deliberately dried up reservoirs - ponds and lakes. However, it becomes profitable only with large production volumes and the presence of a sufficient number of the above reservoirs.
However, despite the apparent difficulty in tracking and regulating the cost, it exists mostly in descriptions - a well-thought-out and skillfully managed salt production business requires almost no intervention: salt is not just a salable or liquid, but an almost ideal product that has a stable high demand and a virtually unlimited market, capable of absorbing any amount of output produced.
In addition, these products do not deteriorate and officially have an infinite shelf life.
The profitability of table salt production may seem low, primarily because of its price, but this is a false feeling: such a business will pay back any investment in the shortest possible time.
Technology and equipment for the production of table salt
Despite the apparent simplicity - rock salt itself is mined in almost pure form - the production of table salt requires a certain set of well-assembled and configured equipment, the quality of the resulting products and, ultimately, the profitability of the enterprise as a whole depend on the correct operation of which.
In this case, we will consider two options for equipment with similar indicators: raw material costs 1100-1150 kg per ton of product; water consumption 90-150 liters per ton of product; energy consumption of 20-30 kWh per ton of product; fuel consumption (coal, gas, diesel) of 10 kg per ton of products and a staff of 2-5 people.
Both lines are made in China by different manufacturers and differ, except for the price - 1,600,000 yuan (about 7.77 million rubles) in the first case and 2,300,000 yuan (about 11.17 million rubles) - in the second - in the range of products: the first line produces coarse edible salt, and the second, both coarse and fine (the so-called "extra") iodized or without the addition of iodine - i.e. only 4 types: large iodized, large without iodine, small iodized and small without iodine.
In addition, during the explanation of salt production technology, all prices for individual components of the production line will be given for a rough estimate of the cost of self-assembly.
As you know, no mineral is found in its pure form. Halite is no exception: foreign inclusions in the form of earth, sand, stones, metal parts, etc. is a common occurrence for him.
Therefore, raw salt, entering the processing plant, goes through several stages of purification: two washes of various types with subsequent crushing (one for coarse salt) and two without crushing (one for coarse salt).
In addition, a special magnetic separator screens out metal impurities.
For the equipment of the first stage of processing, you will need
- raw salt hopper with a capacity of 5 cu. m (price - 29,000 yuan, or about 140.9 thousand rubles),
- spiral conveyor (price - 28,000 yuan, or about 136 thousand rubles),
- belt conveyor (price -52,000 yuan, or about 252.6 thousand rubles),
- magnetic separator (price -5,000 yuan, or about 24.3 thousand rubles),
- spiral washing for salt (price - 78,000 yuan, or about 378.9 thousand rubles),
- roller crusher (price - 82,000 yuan, or about 398.3 thousand rubles),
- interfering salt washer (price - 73,000 yuan, or about 354.6 thousand rubles),
- a special industrial pump for salt (price - 41,000 yuan, or about 199.2 thousand rubles),
- brine tank (price - 14,000 yuan, or about 68 thousand rubles)
- and two pumps for brine (price - 12,000 yuan each, or about 116.6 thousand rubles for both), equipped with a special seal that is resistant to aggressive (salt) environments worth 3,000 yuan, or 14.6 thousand rubles.
Salt purified from impurities is dried using an industrial centrifuge (265,000 yuan, or about 1,287.3 thousand rubles).
Then, depending on the type of product chosen, the semi-finished product is sent either to the iodine addition unit (43,000 yuan, or about 208.9 thousand rubles) to obtain iodized salt, or, through an additional spiral conveyor (41,000 yuan, or about 199.2 thousand rubles) directly into a vibration dryer (145,000 yuan, or about 704.4 thousand rubles) - to obtain coarse iodized salt and coarse salt without the addition of iodine.
If the selected type of table salt is fine, then after passing through the unit for adding iodine and vibration drying, it is subjected to additional crushing in a roller crusher (72,000 yuan, or about 349.8 thousand rubles).
Just as in the previous case, the iodization stage is optional - depending on whether fine salt should be iodized or not, it is added or excluded in manufacturing process.
The final drying of the salt is carried out with the help of hot air formed in the oven (150,000 yuan, or about 728.7 thousand rubles), pumped with an industrial fan (19,000 yuan, or 92.3 thousand rubles).
However, the list of drying equipment is not limited to these two positions: in addition to the blower, you also need a cooling fan (5,000 yuan, or about 24.3 thousand rubles), an extractor for exhaust air (18,000 yuan, or 87.4 thousand rubles). .), additional 3 sets of spiral conveyors (41,000 yuan each, or about 597.5 thousand rubles for everything) to move salt between units, a rotating sieve to separate salt fractions that do not meet the fine salt standard (84,000 yuan , or about 408 thousand rubles), as well as a dust extractor (34,000 yuan, or about 165.2 thousand rubles), respectively, for salt ground into dust, which also should not be present in the final product. At the same stage, other excipients are added to the salt (also optional), for example, potassium ferrocyanide (E536 in the European food additive coding system) - a non-poisonous complex salt - as an agent that resists caking of table salt.
In addition, it is possible to add other excipients - up to about 97-98% sodium chloride content.
Most often, iodides, carbonates are added, and in recent times- fluorides. Fluoride supplementation, for example, is used to prevent dental disease.
After adding auxiliary substances, another spiral conveyor (41,000 yuan, or about 199.2 thousand rubles) delivers the finished salt of both types to a special bunker (39,000 yuan, or about 189.4 thousand rubles), from where they fall to a semi-automatic packer (85,000 yuan, or about 412.9 thousand rubles), and then to a box packing line (5,000 yuan, or about 24.3 thousand rubles) and, after passing the test at automatic control measuring instruments (scales, quality control of individual and group packaging, etc., a line with a total price of 6,000 yuan, or about 29.1 thousand rubles) are shipped to the finished product warehouse.
The above list of table salt production equipment is complete. But additional nodes and details are not listed, the task of which is to link the parts of the line together.
These include:
- connecting devices for electrical wires (105,000 yuan, or about 510.1 thousand rubles),
- thermal insulation material (26,000 yuan, or about 126.3 thousand rubles),
- valves for connecting pipes (35,000 yuan, or about 170 thousand rubles),
- coil (10,000 yuan, or about 48.6 thousand rubles),
- a set of connecting pipes (3,000 yuan, or about 14.6 thousand rubles)
- and the control panel itself (75,000 yuan, or about 364.3 thousand rubles).
With regard to ready-made lines, we can say that their purchase (as a rule, together with the assembly service, usually carried out by the specialists of the issuing enterprise) will cost a little more than a line purchased by individual nodes and assembled on their own.
On the other hand, in this moment there is also a minus: when purchasing nodes one by one, it is easier to choose more reliable units for the most critical areas, while the quality of the units present in the line set corresponds to the quality of the worst of them - after all, if it fails, the entire technological chain will stop, the strength of which depends from the strength of its weakest link.
The productivity of one line is 1 ton per hour (net weight, i.e. without packaging), so one-shift work is possible at first, but then, with the development of the business, it is possible to switch to two- or three-shift.
Prospects for the development of the salt production business
Almost all prospects for the development of salt production are prospects for a linear expansion of the volume of output. But actually, that's not all.
Firstly, now there is a (still weak in Russia) a small market trend - the so-called. "low sodium salt" (English low sodium salt). Most of these products are mixtures of sodium chloride with potassium or magnesium chlorides. It is possible to launch such a production.
Another promising direction is the parallel launch chemical production: table salt is also used to produce soda, chlorine, hydrochloric acid, sodium hydroxide and metallic sodium.
In addition, if your deposit contains not only halite, but also sylvinite, then it is possible to slightly equip the production by equipping the main line with an auxiliary one: sylvinite is a raw material for the production of potassium chloride, which is used as an agricultural fertilizer.
Productivity 1 t/h. Salt (sodium chloride) is important element ensuring the life of man and the animal world. Salt production, since ancient times, was considered a profitable and noble business.
We offer you to choose a complete set of the salt production plant that best meets your requirements.
We have three plant configurations: Econom, Standard and Full.
Distinctive features of the Econom configuration is the maximum use of conditions natural environment. This plant has low energy consumption. Technological process susceptible to changing conditions environment. Reacts negatively to changes or deterioration in the chemical composition of salt, incl. insoluble impurities. The products produced are of varying quality and a high level of manual labor. Requires constant quality control. The production cycle of finished products is 7-14 days.
The Standard package is the best offer for manufacturers working on raw materials with high characteristics of the feedstock. In this configuration, the method of double purification of raw materials is used, which makes it possible to produce products High Quality. The line is semi-automatic. Has a low rate of manual labor. The production cycle is 4-6 hours. Let out production corresponds to GOST, and also allows to trade with large federal customers and to sell salt for Export to the countries of the former CIS.
The Full package has the highest automation ratio. Production of products is based on the method of deep processing of raw materials. This line is susceptible to severe pollution, which allows you to trade with the largest foreign customers. The production cycle is 4-6 hours. Production complies with ISO quality standards. Finished products corresponds to GOST. This configuration allows you to trade with large federal customers and sell salt for export to the countries of the former CIS, as well as the countries of the Near and Far Abroad.
Plan-scheme of the Econom assembly plant
Plan-scheme of the plant of the Standard and Full configuration
Conclusion: in terms of return on investment, the Econom equipment line looks the most attractive. It has the smallest amount of initial investment, with the fastest return on investment Money. However, when choosing a configuration, it is also necessary to take into account the dependence of the production process on external factors.
Plants with Standard and Full equipment are much more resistant to changes in external factors, and therefore have a more stable production process. This, in turn, makes it possible to achieve a constant high quality of products and, as a result, the possibility of trading with large customers.
The client needs to independently assess the market in which he is going to work and who his potential client is. Further, based on this, choose the most complete package that suits you.
Salt production is a very good business idea. Salt is always a tradable and rather liquid commodity, which practically does not deteriorate, has a constant demand and an infinite shelf life. All these qualities indicate that salt is an ideal commodity, and salt processing and its subsequent sale is a good and cost-effective idea to start your business.
But the production process directly depends on the type of salt itself.
One of the healthiest is sea salt. It contains various very useful minerals. Sea salt is obtained by evaporating sea water, because it contains a huge list of salts with various additives.
If doing salt production, then in this case it is necessary to carefully consider business plan
.
In order to obtain table salt, halite, or rock salt, is needed. Basically, first they develop halite deposits, and then, after a whole specific processing process, table salt is obtained from the mined rock salt. But besides this method, the evaporation of salt from salt water is also practiced. It can be both sea water and water of saline reservoirs - lakes or ponds. However, this alternative method becomes profitable only in cases of a large number of the above reservoirs.
Halite is the mineral from which table salt is made. It, like any mineral, contains foreign inclusions in the form of sand, earth or some metal parts. For this reason, as soon as raw salt enters the plant, it first goes through several stages of purification. First, it is washed twice with various types of devices, then it goes through the crushing stage, and at the end it is washed twice again. At the same time, the magnetic separator screens out metal impurities that may be in the halite. After the salt has passed the stage of purification from impurities, it is dried using a special centrifuge.
In order to obtain large iodized salt, the resulting semi-finished product is sent to the unit for adding iodine, and then to vibration drying. If coarse salt should not be iodized, then the step of adding iodine is skipped, and the salt directly enters the vibration dryer. In the event that fine table salt is needed, then after the semi-finished product has passed the stage of adding iodine and vibration drying, it is sent to the crusher. If the fine salt is not to be iodized, then this processing step is excluded from the production process.
After the process of adding iodine and crushing, the salt is dried. This happens with the help of hot air, which is blown into the furnace by an industrial fan. Also, at this stage, you can add other excipients. These may be some food additives that resist caking of table salt, iodides, carbonates, fluorides. Fluoride supplementation is useful for preventing dental disease. At the same time, the total amount of food additives in salt should not exceed 2-3% (as a percentage).
After all auxiliary substances are added to the salt, it is completely ready for packaging.
Video - how sea salt is mined and produced:
The raw brine from the brine field continuously enters the raw brine tank pos. E18 with a capacity of 2000 m3. From the tank by centrifugal pumps type X 200-150-400 pos. H29 is supplied for heating to a group of heat exchangers. In the heat exchangers pos. T4 brine is heated up to 40ºC due to the heat of the condensate from the secondary steam of the evaporators.
After passing the heating unit, the brine enters the central part of the sump damper pos. X10, where it is mixed with a soda-caustic reagent and a working solution of PAAG. The settling tank piping scheme provides for their operation in autonomous and sequential mode. Soda-caustic reagent is supplied in the amount of 0h8 m3/hour.
After mixing the crude brine and the soda-caustic reagent, sparingly soluble compounds are formed: calcium carbonate CaCO3 and magnesium hydroxide Mg(OH)2. The solubility of calcium carbonate decreases with increasing temperature, and therefore, to reduce the residual content of calcium ions, it is recommended to clean the brine at a temperature of 30-40ºC. In addition, as the temperature rises, larger and well-settling calcium carbonate crystals are formed, which is very important for the subsequent settling of the brine.
Purified brine must contain:
CaI+ ions not more than 0.05 g/dmi;
MgI+ ions not more than 0.04 g/dmі;
excess CO3ІЇ not more than 0.15 g/dm³;
excess OH is not more than 0.1 g/dmi.
In the sump, CaCO3 and Mg(OH)2 are formed and the brine is clarified from these sediments. Settling tanks are single-tiered with a central rake drive and a central inlet of the liquid to be settled.
Through a drain funnel installed in the upper peripheral part of the drain trough of the sump (in sequential mode of operation), the clarified brine flows by gravity into the tanks of the purified brine pos. E20 with a capacity of 2000 m3 each.
To intensify the sludge process of the treated brine, PAAG is used with a working concentration of 0.001-0.1%, which is fed into the settling tanks thickeners by pumps pos. H30. The sludge from the sedimentation tanks, thickening, continuously descends into the sludge collector pos. E19. Sludge from the collections, partially diluted with water 1:10 to a solid phase concentration of up to 18%, goes to the sludge storage.
Brine purified from calcium and magnesium salts in an amount of up to 240 m3 from tanks by centrifugal pumps of the X280 / 29T type pos. H32 is supplied to the evaporation section and in the amount of 25-100m3 per shift to the reagent section for the preparation of reagents.
Three evaporators are installed in the evaporator section, including one standby one.
The initial purified brine in the amount of up to 240 m³/hour (based on two working evaporators) with a temperature of 18-35ºC from the tanks with pumps of the X 280/29-T type, pos. H32 is fed into the feed tanks pos. E21 with a capacity of 100 m3 each, part of the purified brine in the amount of 25-40 m3/hour is sent to the centrifugation department for salt washing in brandes thickeners and centrifuges.
The recirculating mother brine is also supplied to the feed tanks in the form of a part of the drain from the Brandes thickeners and centrifuge centrifuge.
The mixture of the initial purified brine with the recirculating mother brine necessary to remove the solid phase from the installation called the feed brine is fed respectively to each evaporator unit pos. K6 in parallel to all evaporators.
Before being fed into the evaporator, the feed brine is heated in a shell-and-tube heat exchanger pos. T5 with a heat exchange surface of 75 m².
The heating of the feed brine before it is fed into the 1 evaporator of the evaporator plant is carried out by the condensate of the heating steam of the 1st building and the secondary steam of the 2nd-4th buildings. The brine moves through the pipe space, the condensate from the heating chambers - through the annulus. The main flow of the feed brine is fed into the irrigation rings located in the upper part of the separators of the evaporators, a small part of this brine in the amount of 2-4 m3/hour is fed into each of the surge tanks to prevent the deposition of common salt on them.
During evaporation in the apparatuses, salt crystallization occurs, while the flow rate of the feed brine in each apparatus is set so (24-32 m³ / h) that the mass fraction of the solid phase in the stripped off suspension (pulp) of each evaporator is equal to 30-40%. At a mass fraction below 30%, the cost of heating steam for obtaining salt increases and salt deposits form on the walls of the evaporator separator, which leads to a reduction in the interwash period of the evaporator. With a mass fraction above 40%, the heat transfer in the evaporators deteriorates and the productivity of the evaporator decreases, in addition, the size of salt crystals decreases.
The evaporated pulp flows from body to body by gravity through the overflow tank. This is facilitated by a consistent decrease in pressure across the housings. The decrease in pressure leads to partial self-evaporation of the solution in subsequent vessels and additional release of secondary vapor in them.
From the fourth (last) evaporator production saline pulp containing 30-40% of the mass. crystalline table salt, in the amount of 60-90 m³ / hour with a pump type GrT 160/31.5 pos. H31 is pumped to the centrifugation department in thickeners of the "Brandes" type pos. X11.
The pressure in the heating chamber of the first evaporator is maintained in the range of 0.15-0.22 MPa. Steam consumption per evaporator unit is up to 30 t/h.
The secondary steam from the first evaporator enters the heating chamber of the second evaporator, the pressure in which should not exceed 0.7 MPa. Subsequent evaporators are heated by the secondary steam of the previous evaporator. From the fourth evaporator, the secondary steam enters a barometric condenser with a diameter of 2.0 m.
The condensate of the heating steam of the first evaporator is cooled in heat exchangers, then pumped out to the boiler room.
Secondary steam condensate from the heating chamber of the second evaporator enters the heating chamber of the third evaporator, and then from it to the heating chamber of the fourth evaporator, from where it is supplied to other production needs.
For the utilization of vapors and non-condensed gases in barometric condensers, recycled water with a temperature not exceeding 28ºC is used. Heated water from barometric condensers enters tanks - water seals with a capacity of 10 m³ each with a temperature not exceeding 50ºC and is then fed to fan cooling towers. Chilled water is collected in a cold water receiver and fed to vapor recovery in barometric condensers.
Non-condensable gases from the heating chamber of the first evaporator are discharged into the heating steam pipeline of the second evaporator. From the heating chamber of the second evaporator, non-condensable gases are discharged to the heating steam pipeline of the third evaporator, from the third heating chamber to the heating steam pipeline of the fourth evaporator, and from the fourth heating chamber to the barometric condenser. The outlet is made through the central pipe located in the annulus of the heating chamber.
Thickening of the salt pulp from 30-40% to 40-60% of the mass. on the solid phase is carried out in thickeners of the "Brandes" type, and the separation of the solid phase - on the filtering horizontal centrifuges of the type S FGP 1201T-01 pos. C23 with pulsating sludge discharge. Washing of salt from the mother brine is carried out with purified brine in thickeners of the "Brandes" type. The consumption of purified brine for washing is 25-35 m 3 /hour. Washed and centrifuged salt with a moisture content of 2-3% of the mass. goes to conveyor belts. Wet salt on the conveyor is treated with a solution of potassium ferrocyanide (PCC) as an anti-caking agent.
The FCC solution is prepared in a tank, where a sample of crystalline potassium ferrocyanide, condensate and compressed air are supplied to mix and dissolve the FCC. From the tank, the FCC solution flows by gravity through the pipeline through the nozzles to the wet salt conveyor pos. Fri 24. Passing through the conveyor, the salt is partially mixed and fed to the dryer.
The flow rate of the FCC solution is controlled automatically, depending on the amount of salt entering the conveyor. Salt consumption is determined using scales (indicator scales) on the conveyor.
Wet table salt with a content of 2.5 ± 0.5% of the mass. Н2О and a temperature of 40 ± 5ºС are distributed by conveyors to bunkers pos. x12. From the bunker, table salt is fed by a feeder and a mechanical caster into the "fluidized bed" apparatus pos. T3, where salt is dried with hot air. Air is supplied to the apparatus by a pipe blower after preheating in the air heater pos T1.
The air is supplied to the air heater in the amount of 11000 ± 2000 nm/h for one drying unit at a pressure of 4000 ± 500 Pa.
In the air heater, the air is heated by flue gases from the combustion of natural gas in burners of the GMG type - 2 M furnaces pos. T 2. When the gas is turned off, high-sulphur fuel oil grade M-100 can be used as fuel. Before combustion, fuel oil is heated by steam at a pressure of 0.6 MPa to 120°C. Air for burning fuel oil, gas (for the burner), for cooling the vaults of the furnace afterburning is supplied by a fan of the VDN type - 11.2 pos. B 33-34 under a pressure of 2000 ± 500 Pa. In this case, the air flow rate for the burners is 5000 ± 1000 nmi/h, and for blowing the vaults and afterburning - 1600 ± 200 nmi/h.
Combustion of natural gas or fuel oil in the furnace occurs at a discharge of 50 ± 20 Pa and temperatures up to 1300ºC. The specified vacuum is maintained by a smoke exhauster pos. B36.
A decrease in vacuum can lead to the release of hot flue gases into the room, an increase in vacuum leads to an increased suction of cold air into the furnace, which can lead to a breakdown of the torch.
Furnace (flue) gases in the mixing chamber of the furnace pos. T2 are mixed with exhaust (after the air heater) return flue gases having a temperature of 180 ± 10ºC. As a result of mixing, the temperature of the flue gases decreases to 550 ± 50ºС, with this temperature they enter the pipe space of the air heater to heat the drying agent, where they are cooled from 550 ± 50ºС to 180 ± 10ºС, and injected into the packed adsorber pos. K8, where gases are cleaned from sulfur-containing compounds, after which the latter are smoked with a DN-12.5 smoke exhauster N = 75 kW, n = 1500 rpm with a capacity of 37000 m3 / h pos. X13 are emitted into the atmosphere through a common gas duct and two chimneys with a diameter of 600 mm. The height of the first chimney is 45 m, the height of the second chimney is 31.185 m. Reducing the temperature of flue gases below 170ºС leads to the formation of acid corrosion of gas pipelines and chimneys, and an increase in temperature above 200ºС leads to failure of the smoke exhauster. Part of the cooled flue gases is supplied by the same smoke exhauster to the furnace mixing chamber to maintain their temperature in front of the air heater in the range of 550 ± 50ºС.
Adsorber pos. K8 is irrigated with soda. The resulting wastewater are sent to the collection of industrial waste pos. E16, from where they are thrown into the sewer.
Dried table salt from the apparatus "KS" through the overflow chute enters the apparatus "KS" for cooling. Air for cooling is supplied to the apparatus by a fan. Cooled table salt is unloaded onto the conveyor pos. PT27, from where it is fed to vertical elevators of the TsG type - 400 pos. PT28 and further to electromagnetic vibrating screens for separating the pellet formed during drying.
Large salt particles (more than 1.2 mm) and lumps that have not passed through the holes in the sieve fabric of vibrating screens pos. E22, descend from it and by gravity in the amount of 320 ± 50 kg / h enter a vertical mixer with a capacity of 10 m і to dissolve the okata pos. E14.
The solution formed in the amount of 3-6 m і 5-10% is pumped out by pumps of the type AX 45/54 into the collection of industrial waste pos. E15.
Magnetic traps are installed on conveyors at the site for pouring salt from vibrating screens onto conveyors. Installation is made in 2 tiers: upper -3 magnets, lower -4 magnets. The main flow of salt with particle sizes less than 1.2 mm is fed to inclined belt conveyors KLS - 800 pos. PT26 supplying salt to the salt packing and packing shop.
The dusty air leaving the apparatus "KS" enters the gas cleaning system. Cleaning is carried out in two stages: preliminary cleaning from the largest particles is carried out in cyclones pos. K7 and cleaning from fine dust particles in the bag filter pos. F9.
The spent drying agent with =70±10ºС and dust content of 12-50 g/nm³ under a discharge of 200±50 Pa is fed into a battery cyclone for cleaning. The air purified in the battery cyclone to a concentration of 12-17g/nm³ t=68±8ºС in the amount of (16±4)x10³nm³/hour under a discharge of 1500±500Pa is sucked in by the fan pos. B35 and is fed under a pressure of 4500 ± 500 Pa for cleaning into a bag filter.
Salt dust is removed from the battery cyclones with the help of chutes equipped with flashing lights (sluice gates) and fed into the container pos. E17, where recycled water enters. The resulting saline water is directed to a pit located in the brine field. Fine dust trapped in the bag filter is fed to the belt conveyor pos. PT25, from where it enters the washout tank.
The spent drying agent finally cleaned of the smallest particles of salt dust at a temperature of 110ºC is fed into the air heater pos. T1, where it is heated to a temperature of 300ºC and returned to the "KS" dryer.
The technological scheme for the production of sodium chloride is presented in Appendix C.
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