CN214693740U - A device that is used for nitrosyl sulfuric acid waste liquid to purify concentrated processing - Google Patents
A device that is used for nitrosyl sulfuric acid waste liquid to purify concentrated processing Download PDFInfo
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Abstract
The utility model discloses a device for purifying and concentrating nitrosyl sulfuric acid waste liquid, wherein a hydrolysis working section is used for mixing nitrosyl sulfuric acid waste liquid and a certain amount of pure water for hydrolysis under the condition of negative pressure, generated nitrogen dioxide gas enters a purification unit for further neutralization and purification absorption treatment, and generated dilute sulfuric acid enters an evaporation and concentration working section; the evaporation concentration section heats the aqueous solution containing sulfuric acid and other solutes in a vacuum state to evaporate volatile substances in the solution together with water, a condenser condenses the volatile substances and the water by using cooling water to form a condensate, and the concentration of the sulfuric acid which is a non-volatile solute in the solution is increased along with the reduction of the volume of the solution to form finished sulfuric acid with the sulfuric acid concentration being more than or equal to 85 percent. The hydrolysis working section and the concentration working section of the device are carried out under the negative pressure vacuum condition, the evaporation temperature is low, the corrosivity to the material of the equipment pipeline is low, the continuous and stable production can be ensured, the energy consumption is effectively reduced, the leakage of acid gas is effectively avoided, and the environmental protection benefit is obvious.
Description
Technical Field
The utility model relates to a waste sulfuric acid treatment technical field, concretely relates to a device that is used for nitrosyl sulfuric acid waste liquid to purify concentrated processing.
Background
The sulfuric acid is widely applied to the industries of chemical engineering, steel and the like. In many production processes, the utilization rate of sulfuric acid is low, and a large amount of sulfuric acid is discharged along with acid-containing wastewater. If the waste water is discharged into the environment without being treated, the water body or the soil can be acidified, the ecological environment is harmed, and a large amount of resources are wasted.
The sulfuric acid waste liquid discharged by any industry has the characteristics of high acid concentration, high corrosivity, high environmental pollution and the like, and is managed by various countries as hazardous waste at present. China puts it in the national records of dangerous waste. The main harm caused by illegal discharge of the sulfuric acid waste liquid is as follows: corroding hydraulic structures such as sewer pipes and reinforced concrete; crops are withered, and the growth of aquatic crops is influenced; when the sulfuric acid waste liquid permeates into the ground, carbonate, sulfite, sulfide and the like in rock and soil react to generate harmful gases such as sulfur dioxide, hydrogen sulfide and the like, and the harmful gases are emitted into the air to pollute the atmosphere; when the fertilizer permeates into soil, soil calcification can be caused after a long time, and the loose state of a soil layer is damaged, so that the growth of crops is influenced; can kill fish; people and animals can drink the water polluted by the pollution to cause gastrointestinal inflammation and even burn; the pollution to water, the poison to organisms and the final damage to human health are all huge. According to the national environmental regulations, the sulfuric acid waste liquid is not allowed to be directly discharged. If the generated sulfuric acid waste liquid is discharged after being treated briefly, a large amount of alkali is added in the treatment process, so that a large amount of dangerous waste sludge is generated and must be treated outsourcedly, high treatment cost is required to be borne, the resource recycling policy is not met, and the resource and cost are greatly wasted. If delivered to a company with hazardous waste disposal qualifications, the huge disposal cost is a huge production cost for the acid production enterprises.
At present, a plurality of treatment methods for waste sulfuric acid exist at home and abroad, and a proper treatment technology needs to be selected according to the specific characteristics of different waste sulfuric acids and the conditions of enterprises. The currently used methods mainly comprise a neutralization method, a high-temperature cracking method, a vacuum concentration method, a chemical oxidation method, a polymerization method, an extraction method, a natural crystallization-diffusion dialysis method, an immersion combustion high-temperature crystallization method, a vacuum concentration freezing crystallization method, an acid adding freezing crystallization method and the like.
Because of the special properties of the waste nitrosyl sulfuric acid liquid and the characteristics of producing nitric acid and nitrogen dioxide by decomposing in water, the waste nitrosyl sulfuric acid liquid is easy to cause safety problems in the processes of external transportation and transferring. However, the treatment method has pertinence to each component in the waste sulfuric acid solution, and the direct application of the treatment method to the treatment of the nitrosyl sulfuric acid waste solution has certain potential safety hazards. Therefore, it is necessary to design a device dedicated for purifying and concentrating the waste nitrosyl sulfuric acid solution, so as to maximally recycle the sulfuric acid resources and avoid the pollution and damage of the waste nitrosyl sulfuric acid solution to the environment.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the defect that exists among the prior art, provide a device that is used for nitrosyl sulfuric acid waste liquid to purify concentrated processing, the device meets the characteristic design of water decomposition output nitric acid, nitrogen dioxide according to nitrosyl sulfuric acid waste liquid, specifically including the workshop section of hydrolysising and concentrated workshop section: the hydrolysis section is to mix and hydrolyze the nitrosyl sulfuric acid waste liquid with a certain amount of pure water under the negative pressure condition, the generated nitrogen dioxide gas enters a purification unit to be further neutralized, purified and absorbed by using a sodium hydroxide solution with the content of 10 percent, and the generated dilute sulfuric acid enters an evaporation concentration section to be subjected to negative pressure solvent evaporation; the basic principle of the evaporation concentration section is that an aqueous solution containing sulfuric acid and other solutes is heated in a vacuum state to evaporate volatile substances in the solution together with water, a condenser condenses the volatile substances and the water to form a condensate, and simultaneously, as the volume of the solution is reduced, the concentration of the non-volatile solute sulfuric acid in the solution is increased to form finished sulfuric acid with the sulfuric acid concentration being more than or equal to 85%. The hydrolysis working section and the concentration working section of the device are carried out under the negative pressure vacuum condition, the evaporation temperature is low, the corrosivity to the material of the equipment pipeline is low, the continuous and stable production can be ensured, the energy consumption is effectively reduced, the leakage of acid gas is effectively avoided, the operation environment is improved, and the environmental protection benefit is obvious.
In order to realize the purpose, the technical scheme of the utility model is to design a device for purifying and concentrating nitrosyl sulfuric acid waste liquid, which comprises a hydrolysis unit, a purification vacuum unit, an evaporation concentration unit and an evaporation vacuum unit, wherein the hydrolysis unit comprises a raw liquid tank, a hydrolysis kettle, a hydrolysis condenser and a hydrolysis condensate tank, a discharge port of the raw liquid tank is connected with a feed inlet of the hydrolysis kettle through a feed pump, a gas outlet of the hydrolysis kettle is connected with a gas inlet of the hydrolysis condenser, a condensate outlet of the hydrolysis condenser is connected with a feed inlet of the hydrolysis condensate tank, a gas outlet of the hydrolysis condensate tank is connected with a gas inlet of the hydrolysis condenser, a shell pass of the hydrolysis condenser is connected with external circulating cooling water, and hydrolysis condensate inside the hydrolysis condensate tank is discharged outside through the hydrolysis condensate pump, an air inlet of a jacket on the hydrolysis kettle is connected with raw steam from the outside, and the raw steam from the outside is discharged or recycled after heat exchange and condensation through the jacket of the hydrolysis kettle;
the purification unit comprises a neutralization tower and a purification tower, wherein a gas inlet of the neutralization tower is connected with a gas outlet of a hydrolysis condenser in the hydrolysis unit, a gas outlet of the neutralization tower is connected with a gas inlet of the purification tower, a liquid outlet at the bottom of the neutralization tower is connected with or discharged outside a spray opening at the top of the neutralization tower through a neutralization tower absorption liquid pump, and a liquid outlet at the bottom of the purification tower is connected with or discharged outside a spray opening at the top of the purification tower through a purification tower absorption liquid pump;
the purification vacuum unit comprises a hydrolysis gas-liquid separation tank and a hydrolysis vacuum unit, wherein a gas inlet of the hydrolysis gas-liquid separation tank is connected with a gas outlet at the top of a purification tower in the purification unit, a gas outlet of the hydrolysis gas-liquid separation tank is connected with the hydrolysis vacuum unit, and a shell pass of the hydrolysis vacuum unit is connected with external circulating cooling water;
the evaporation concentration unit comprises an evaporator, a separator, a steam saturator, a condenser, a noncondensable gas condenser, a condensate cooler, a concentration liquid condenser, a hot water preheater and a condensate tank, wherein the shell pass of the evaporator is connected with the shell pass of the hot water preheater, raw steam from the outside is discharged or recycled after sequentially passing through the shell pass of the evaporator and the shell pass of the hot water preheater, a liquid inlet of the hot water preheater is connected with a shell pass liquid outlet of the concentration liquid condenser, a shell pass liquid inlet of the concentration liquid condenser is connected with a discharge hole of a hydrolysis kettle in the hydrolysis unit through a hydrolysis discharge pump, a liquid outlet of the hot water preheater is connected with a liquid inlet of the separator, a circulating liquid outlet of the separator is connected with a liquid inlet of the evaporator through a circulating pump, and a liquid outlet of the evaporator is connected with a circulating liquid inlet of the separator, the liquid outlet of the separator is connected with the liquid inlet of the concentration liquid condenser through a discharge pump, and the liquid outlet of the concentration liquid condenser is connected with a finished sulfuric acid tank; the steam outlet of the separator is connected with the air inlet of a steam saturator, the air outlet of the steam saturator is connected with the air inlet of a condenser, and the non-condensable gas outlet of the condenser is connected with the air inlet of the non-condensable gas condenser; the device comprises a steam saturator, a condensate outlet of the steam saturator, a condensate outlet of a condenser and a liquid outlet of a non-condensable gas condenser, wherein the condensate outlet of the steam saturator, the condensate outlet of the condenser and the liquid outlet of the non-condensable gas condenser are all connected with a liquid inlet of a condensate tank, a gas outlet of the condensate tank is connected with a gas inlet of the condenser, the liquid outlet of the condensate tank is connected with a liquid inlet of a condensate cooler through a condensate pump, the liquid outlet of the condensate cooler is respectively connected with a liquid inlet of a hydrolysis kettle in a hydrolysis unit, a spray port of the steam saturator and a spray port of the non-condensable gas condenser, and a shell pass of the condenser and a shell pass of the condensate cooler are all connected with external circulating cooling water;
the evaporation vacuum unit comprises an evaporation gas-liquid separation tank and a vacuum pump, and a gas outlet of a non-condensable gas condenser in the evaporation concentration unit is connected with the vacuum pump through the evaporation gas-liquid separation tank.
The preferred technical scheme is that the evaporator, the hot water preheater and the condenser all adopt high-temperature impregnated graphite heat exchangers, the condensate cooler, the concentrated liquid condenser and the hydrolysis condenser all adopt graphite condensers, and the steam saturator and the non-condensable gas condenser all adopt polypropylene materials.
Further preferably, the hydrolysis kettle adopts a glass lining reaction kettle; the separator adopts a steel lining glass lining separator, and is provided with an independent feed inlet, an observation hole and a liquid level control system for observing and controlling the feed flow.
In a further preferred technical scheme, the hydrolysis discharge pump, the neutralization tower absorption liquid pump, the purification tower absorption liquid pump, the circulating pump and the discharge pump are all made of PFA high-temperature-resistant corrosion-resistant sandwich plate type horizontal pumps; the feeding pump, the hydrolysis condensate pump and the condensate pump are all ultra-high molecular polyethylene high-temperature-resistant corrosion-resistant leakage-free sandwich type engineering plastic horizontal pumps; the vacuum pump adopts an LG series dry-type constant-pitch screw vacuum pump; the hydrolysis vacuum unit is an RPP-280 water jet vacuum unit made of polypropylene.
Further preferably, the hydrolysis condensate tank, the hydrolysis gas-liquid separation tank, the condensate tank and the evaporation gas-liquid separation tank are polypropylene vertical storage tanks.
Further preferably, the neutralization tower and the purification tower adopt an HY-II type full negative pressure polypropylene washing tower.
The utility model has the advantages and the beneficial effects that:
1. the utility model discloses a device in concentrated processing of nitrosyl sulfuric acid waste liquid purification, the device meet the characteristic design of water decomposition output nitric acid, nitrogen dioxide according to nitrosyl sulfuric acid waste liquid, specifically include the workshop section of hydrolysising and concentrated workshop section: the hydrolysis section is to mix and hydrolyze the nitrosyl sulfuric acid waste liquid with a certain amount of pure water under the negative pressure condition, the generated nitrogen dioxide gas enters a purification unit to be further neutralized, purified and absorbed by using a sodium hydroxide solution with the content of 10 percent, and the generated dilute sulfuric acid enters an evaporation concentration section to be subjected to negative pressure solvent evaporation; the basic principle of the evaporation concentration section is that an aqueous solution containing sulfuric acid and other solutes is heated in a vacuum state to evaporate volatile substances in the solution together with water, a condenser condenses the volatile substances and the water to form a condensate, and simultaneously, as the volume of the solution is reduced, the concentration of the non-volatile solute sulfuric acid in the solution is increased to form finished sulfuric acid with the sulfuric acid concentration being more than or equal to 85%. The hydrolysis working section and the concentration working section of the device are carried out under the negative pressure vacuum condition, the evaporation temperature is low, the corrosivity to the material of the equipment pipeline is low, the continuous and stable production can be ensured, the energy consumption is effectively reduced, the leakage of acid gas is effectively avoided, the operation environment is improved, and the environmental protection benefit is obvious.
2. The utility model discloses a device in concentrated processing of nitrosyl sulfuric acid waste liquid purification, its secondary steam pipeline that separates at the separator has installed steam saturator additional, purifies the secondary steam, effectively prevents other material crystallization that spill over in the interior dilute sulfuric acid solution of separator and blocks up the condenser, has guaranteed the security and the reliability of production process.
3. The utility model discloses a in device of nitrosyl sulfuric acid waste liquid purification concentration treatment, the heating steam condensate water of evaporimeter lets in hot water heater through the trap, and the steam loss has been avoided from hot water heater discharge to the condensate water, has also solved the noise pollution of steam trap.
4. The utility model discloses a device for purifying and concentrating nitrosyl sulfuric acid waste liquid, wherein an evaporation concentration unit consisting of an evaporator and a separator adopts forced external circulation evaporation, and has high evaporation intensity and high thermal efficiency; the circulating condensing system consisting of the condenser, the non-condensable gas condenser and the condensate tank has good condensing effect and effectively avoids the leakage of the non-condensable gas and steam.
5. The utility model discloses a in concentrated processing's of nitrosyl sulfuric acid waste liquid purification device, each equipment all adopts resistant vacuum, the good, the strong material of corrosion resistance of weatherability, ensures that the device has advantages such as working property is reliable, safe operation degree is high, maintenance cycle length, long service life, operation maintenance are simple and convenient to acid medium.
Drawings
FIG. 1 is a process flow diagram of a hydrolysis unit, a purification unit and a purification vacuum unit in the device for purifying and concentrating the waste nitrosyl sulfuric acid liquid; in the figure, R201 is a first hydrolysis kettle; r202 and a second hydrolysis kettle; e208, a hydrolysis condenser; t201, a neutralization tower; t202, a purification tower; p201, a feed pump; p202, a hydrolysis discharge pump; p203, a hydrolysis condensate pump; p204, a neutralization tower absorption liquid pump; p205, a purification tower absorption liquid pump; p206, a hydrolysis vacuum unit; v201, a hydrolysis condensate tank; v202, a hydrolysis gas-liquid separation tank;
FIG. 2 is a process flow diagram of an evaporation concentration unit and an evaporation vacuum unit in the device for purifying and concentrating the waste nitrosyl sulfuric acid liquid; in the figure, E201, an evaporator; e202, a steam saturator; e203, a condenser; e204, a non-condensable gas condenser; e205, a condensate cooler; e206, a concentrated solution cooler; e207, a hot water preheater; p207, a circulating pump; p208, a discharge pump; p209, a condensate pump; p210, a vacuum pump; v203, a condensate tank; v204, evaporating a gas-liquid separation tank; s201, a separator.
Detailed Description
The following description will further describe embodiments of the present invention with reference to the accompanying drawings and examples. The following examples are only for illustrating the technical solutions of the present invention more clearly, and the protection scope of the present invention is not limited thereby.
Examples
The device for purifying and concentrating the nitrosyl sulfuric acid waste liquid is mainly used for treating the nitrosyl sulfuric acid waste liquid, designed according to the characteristics of nitric acid and nitrogen dioxide produced by the nitrosyl sulfuric acid waste liquid in water decomposition, and specifically comprises a hydrolysis section and a concentration section:
firstly, adding pure water (or evaporation condensate discharged from a concentration section) accounting for 50% of the weight of the nitrosyl sulfuric acid waste liquid into a hydrolysis kettle in advance under a negative pressure condition, slowly adding the nitrosyl sulfuric acid waste liquid to be treated, heating after the nitrosyl sulfuric acid waste liquid is added, and removing most of nitrogen dioxide in the waste liquid. The nitrogen dioxide enters a neutralization tower and a purification tower, the neutralization and purification are carried out by using a sodium hydroxide solution with the content of 10 percent, and the dilute sulfuric acid after the hydrolysis and purification enters a concentration working section.
The concentration section is mainly used for evaporating the solvent under negative pressure in the dilute sulfuric acid purified in the hydrolysis section, reducing the evaporation temperature and reducing the boiling point in the concentration process of the sulfuric acid, namely, the dilute sulfuric acid is treated by adopting a single-effect negative pressure concentration method, which is essentially a physical process for separating solute from the solvent in the solution, and the basic principle of the process is that an aqueous solution containing sulfuric acid and other solutes is heated under the vacuum state, so that volatile substances in the solution and water are evaporated together, and a condenser is formed by condensing cooling water through a condenser; meanwhile, as the volume of the solution is reduced, the concentration of the non-volatile solute sulfuric acid in the solution is increased, and finished sulfuric acid with the specified concentration is produced.
The device for purification and concentration treatment of nitrosyl sulfuric acid waste liquid in the embodiment specifically combines with the devices shown in fig. 1-2, and comprises a hydrolysis unit, a purification vacuum unit, an evaporation concentration unit and an evaporation vacuum unit, wherein the hydrolysis unit comprises a raw liquid tank, a first hydrolysis kettle R201, a second hydrolysis kettle R202, a hydrolysis condenser E208 and a hydrolysis condensate tank V201, a discharge port of the raw liquid tank is respectively connected with a feed port of the first hydrolysis kettle R201 and a feed port of the second hydrolysis kettle R202 through a feed pump P201, a gas outlet of the first hydrolysis kettle R201 and a gas outlet of the second hydrolysis kettle R202 are both connected with a gas inlet of the hydrolysis condenser E208, a condensate outlet of the hydrolysis condenser E208 is connected with a feed port of the hydrolysis condensate tank V201, a gas outlet of the hydrolysis condensate tank V201 is connected with a gas inlet of the hydrolysis condenser E208, and a shell pass of the hydrolysis condenser E208 is connected with external circulating cooling water, the hydrolysis condensate in the hydrolysis condensate tank V201 is discharged outside through a hydrolysis condensate pump P203, air inlets of jackets on the first hydrolysis kettle R201 and the second hydrolysis kettle R202 are connected with raw steam from the outside, and the raw steam from the outside is discharged outside or recycled after heat exchange and condensation through the jacket of the first hydrolysis kettle R201 or the jacket of the second hydrolysis kettle R202;
the purification unit comprises a neutralization tower T201 and a purification tower T202, wherein a gas inlet of the neutralization tower T201 is connected with a gas outlet of a hydrolysis condenser E208 in the hydrolysis unit, a gas outlet of the neutralization tower T201 is connected with a gas inlet of the purification tower T202, a liquid outlet at the bottom of the neutralization tower T201 is connected with or discharged from a spray opening at the top of the neutralization tower T201 through a neutralization tower absorption liquid pump P204, and a liquid outlet at the bottom of the purification tower T202 is connected with or discharged from a spray opening at the top of the purification tower T202 through a purification tower absorption liquid pump P205;
the purification vacuum unit comprises a hydrolysis gas-liquid separation tank V202 and a hydrolysis vacuum unit P206, wherein a gas inlet of the hydrolysis gas-liquid separation tank V202 is connected with a gas outlet at the top of a purification tower T202 in the purification unit, a gas outlet of the hydrolysis gas-liquid separation tank V202 is connected with the hydrolysis vacuum unit P206, and a shell pass of the hydrolysis vacuum unit P206 is connected with external circulating cooling water;
the evaporation concentration unit comprises an evaporator E201, a separator S201, a steam saturator E202, a condenser E203, a non-condensable gas condenser E204, a condensate cooler E205, a concentrated solution cooler E206, a hot water preheater E207 and a condensate tank V203, wherein the shell pass of the evaporator E201 is connected with the shell pass of the hot water preheater E207, raw steam from the outside sequentially passes through the shell pass of the evaporator E201 and the shell pass of the hot water preheater E207 and then is discharged or recycled, the liquid inlet of the hot water preheater E207 is connected with the shell pass liquid outlet of the concentrated solution cooler E206, the shell pass liquid inlet of the concentrated solution cooler E206 is respectively connected with the discharge hole of a first hydrolysis kettle R201 and the discharge hole of a second hydrolysis kettle R202 in the hydrolysis unit through a hydrolysis discharge pump P202, the liquid outlet of the hot water preheater E207 is connected with the liquid inlet of the separator S201, the circulating liquid outlet of the separator S is connected with the liquid inlet of the evaporator E201 through a circulating pump P207, the liquid outlet of the evaporator E201 is connected with the circulating liquid inlet of the separator S201, the liquid outlet of the separator S201 is connected with the liquid inlet of the concentrated liquid cooler E206 through a discharge pump P208, and the liquid outlet of the concentrated liquid cooler E206 is connected with a finished product sulfuric acid tank; a steam outlet of the separator S201 is connected with an air inlet of a steam saturator E202, an air outlet of the steam saturator E202 is connected with an air inlet of a condenser E203, and a non-condensable gas outlet of the condenser E203 is connected with an air inlet of a non-condensable gas condenser E204; the condensate outlet of the steam saturator E202, the condensate outlet of the condenser E203 and the liquid outlet of the non-condensable gas condenser E204 are connected with the liquid inlet of a condensate tank V203, the gas outlet of the condensate tank V203 is connected with the gas inlet of the condenser E203, the liquid outlet of the condensate tank V203 is connected with the liquid inlet of a condensate cooler E205 through a condensate pump P209, the liquid outlet of the condensate cooler E205 is respectively connected with the liquid inlet of a first hydrolysis kettle R201, the liquid inlet of a second hydrolysis kettle R202, the spray opening of the steam saturator E202 and the spray opening of the non-condensable gas condenser E204 in the hydrolysis unit, and the shell side of the condenser E203 and the shell side of the condensate cooler E205 are connected with external circulating cooling water;
the evaporation vacuum unit comprises an evaporation gas-liquid separation tank V204 and a vacuum pump P210, and a gas outlet of a non-condensable gas condenser E204 in the evaporation concentration unit is connected with the vacuum pump P210 through the evaporation gas-liquid separation tank V204.
Preferably, the evaporator E201, the hot water preheater E207 and the condenser E203 all adopt high-temperature impregnated graphite heat exchangers, the condensate cooler E205, the concentrated solution cooler E206 and the hydrolysis condenser E208 all adopt graphite condensers, and the steam saturator E202 and the non-condensable gas condenser E204 all adopt polypropylene materials.
Further preferably, the first hydrolysis kettle R201 and the second hydrolysis kettle R202 both adopt glass lining reaction kettles; the separator S201 adopts a steel lining glass lining separator, and the separator S201 is provided with an independent feed inlet, an observation hole and a liquid level control system for observing and controlling the feed flow.
Further preferably, the hydrolysis discharge pump P202, the neutralization tower absorption liquid pump P204, the purification tower absorption liquid pump P205, the circulating pump P207 and the discharge pump P208 are all made of PFA sandwich plate type horizontal pumps resistant to high temperature and corrosion; the feed pump P201, the hydrolysis condensate pump P203 and the condensate pump P209 are all made of ultra-high molecular polyethylene high-temperature-resistant corrosion-resistant non-leakage sandwich type engineering plastic horizontal pumps; the vacuum pump P210 adopts an LG series dry-type constant-pitch screw vacuum pump; the hydrolysis vacuum unit P206 is an RPP-280 water jet vacuum unit made of polypropylene.
Further preferably, the hydrolysis condensate tank V201, the hydrolysis gas-liquid separation tank V202, the condensate tank V203, and the evaporation gas-liquid separation tank V204 all adopt polypropylene vertical storage tanks.
Further preferably, an HY-II type full negative pressure polypropylene washing tower is adopted for both the neutralization tower T201 and the purification tower T202.
According to the device for purifying and concentrating the nitrosyl sulfuric acid waste liquid, according to the characteristic that the nitrosyl sulfuric acid waste liquid is decomposed in water to produce nitric acid and nitrogen dioxide, firstly, the nitrosyl sulfuric acid waste liquid is subjected to decomposition reaction with water in a hydrolysis kettle of a hydrolysis section, and the produced nitrogen dioxide enters a neutralization tower and a purification tower to be neutralized and purified by using a sodium hydroxide solution with the content of 10%; the dilute sulfuric acid after hydrolysis and purification enters an evaporation unit of a concentration section, is heated in a vacuum state to evaporate volatile substances in the solution and water together, and is condensed by a condenser by utilizing cooling water to form condensate; meanwhile, along with the reduction of the volume of the solution, the concentration of the sulfuric acid which is a non-volatile solute in the solution is increased, and finished sulfuric acid with the sulfuric acid concentration being more than or equal to 85% is formed. The device for purifying and concentrating the nitrosyl sulfuric acid waste liquid comprises the following process flows:
1) and material flow:
pure water accounting for 50% of the treatment capacity of the nitrosyl sulfuric acid waste liquid is added into a first hydrolysis kettle R201 and a second hydrolysis kettle R202, and the nitrosyl sulfuric acid waste liquid discharged from a production workshop is collected, enters a raw liquid tank for precipitation and impurity removal, is metered by a feed pump P201, and then is dripped into the first hydrolysis kettle R201 and the second hydrolysis kettle R202. After the nitrosyl sulfuric acid wastewater is hydrolyzed, the temperature is raised, volatile substances such as nitrogen dioxide and the like are removed to the maximum extent, and gases such as nitrogen dioxide and the like generated in the hydrolysis process sequentially enter a neutralization tower T201 and a purification tower T202. The neutralization tower T201 and the purification tower T202 adopt sodium hydroxide solution with the content of 10% to carry out neutralization and purification treatment. The whole hydrolysis process is completed under the condition of negative pressure, and the purified dilute sulfuric acid enters the evaporation concentration unit through the hydrolysis discharge pump P202.
The purified dilute sulfuric acid enters a separator S201 after being metered, passes through a concentrated solution cooler E206 shell pass and a hot water preheater E207 on the way, and is preheated by respectively utilizing the heat discharged by the concentrated solution and the heat of steam condensate water of an evaporator E201; the feed liquid entering the separator S201 is heated by saturated steam of the evaporator E201, the feed liquid reaching the designed boiling point is subjected to steam-liquid separation in the separator S201, the feed liquid is subjected to multiple forced circulation in an evaporation unit and is subjected to designed evaporation concentration, the feed liquid with the sulfuric acid concentration of more than or equal to 85% is obtained after concentration and is pumped out to a recovered sulfuric acid collecting tank through a discharge pump P208, and the feed liquid passes through a concentrated liquid cooler E206 on the way, is cooled by using dilute sulfuric acid, and simultaneously preheats the dilute sulfuric acid entering the separator S201.
2) And heating steam and condensed water flow:
in the hydrolysis unit, raw steam from the outside enters the jackets of a first hydrolysis kettle R201 and a second hydrolysis kettle R202 after being decompressed, and is discharged outside or reused in a boiler after passing through a drain valve after heat exchange and condensation;
in the evaporation concentration unit, raw steam from the outside enters an evaporator E201 shell pass for heat exchange and condensation, then is discharged outside or recycled after being preheated by a drain valve and a hot water preheater E207, secondary steam generated by a separator S201 enters a condenser E203 for condensation and then enters a condensate tank V203, condensate collected by the condensate tank V203 is pumped into a first hydrolysis kettle R201 and a second hydrolysis kettle R202 through a condensate pump P209 to be used as hydrolysis water, and is cooled by a condensate cooler E205 during the process; the non-condensable gas in the condenser E203 enters a non-condensable gas condenser E204 for cooling and purification, and the condensate after the non-condensable gas is purified returns to the condensate tank V203; the cooled condensate in the condensate tank V203 enters the vapor saturator E202 through the condensate pump P209 to cool the secondary vapor generated in the separator S201 (the secondary vapor is superheated vapor), and the cooling liquid returns to the condensate tank V203.
3) And a vacuum system:
the purification vacuum unit consists of a hydrolysis vapor-liquid separation tank V202 and a purification vacuum unit P206, non-condensable gas in the purification unit is pumped out, the system vacuum of the purification unit is maintained, and effective clean production and the production environment meet the environmental protection requirement.
The evaporation vacuum unit consists of a condenser E203, a vacuum pump P210 and an evaporation vapor-liquid separation tank V204, and is used for pumping out non-condensable gas in the evaporation concentration unit, maintaining the higher vacuum of the evaporation concentration unit and realizing effective high-vacuum low-temperature evaporation.
The device for purifying and concentrating the nitrosyl sulfuric acid waste liquid adopts the working modes of continuous feeding and intermittent discharging, and the evaporation concentration unit mainly adopts vacuum external circulation concentration, so that the evaporation temperature is reduced; secondly, the evaporation speed is improved; thirdly, energy consumption is reduced; fourthly, the crystallization and scaling of the materials are reduced, and the normal operation and the service life of the device are ensured. Other notable features include:
A. the hydrolysis purification concentration technology is adopted to treat the nitrosyl sulfuric acid waste liquid, the technology is reliable, the economy is low, and the method is suitable for the nitrosyl sulfuric acid waste liquid treatment and the resource comprehensive utilization of the nitrosyl sulfuric acid waste liquid in the related industries;
B. the evaporation concentration unit adopts a negative pressure evaporation process, so that the evaporation temperature is reduced, the service life of the equipment is prolonged, and the maintenance cost of the equipment is reduced;
C. the energy consumption is less, and the device for purifying and concentrating the waste nitrosyl sulfuric acid can continuously operate;
D. and a full-automatic control system is adopted, so that the operation personnel is less, the labor cost is reduced, and the operation is simple.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of improvements and decorations can be made without departing from the technical principle of the present invention, and these improvements and decorations should also be regarded as the protection scope of the present invention.
Claims (6)
1. A device for purification and concentration treatment of waste nitrosyl sulfuric acid liquid is characterized by comprising a hydrolysis unit, a purification vacuum unit, an evaporation concentration unit and an evaporation vacuum unit, wherein the hydrolysis unit comprises a raw liquid tank, a hydrolysis kettle, a hydrolysis condenser (E208) and a hydrolysis condensate tank (V201), a discharge port of the raw liquid tank is connected with a feed port of the hydrolysis kettle through a feed pump (P201), a gas outlet of the hydrolysis kettle is connected with a gas inlet of the hydrolysis condenser (E208), a condensate outlet of the hydrolysis condenser (E208) is connected with a feed port of the hydrolysis condensate tank (V201), a gas outlet of the hydrolysis condensate tank (V201) is connected with a gas inlet of the hydrolysis condenser (E208), a shell pass of the hydrolysis condenser (E208) is connected with external circulating cooling water, and hydrolysis condensate inside the hydrolysis condensate tank (V201) is discharged outside through a hydrolysis condensate pump (P203), an air inlet of a jacket on the hydrolysis kettle is connected with raw steam from the outside, and the raw steam from the outside is discharged or recycled after heat exchange and condensation through the jacket of the hydrolysis kettle;
the purification unit comprises a neutralization tower (T201) and a purification tower (T202), wherein the gas inlet of the neutralization tower (T201) is connected with the gas outlet of a hydrolysis condenser (E208) in the hydrolysis unit, the gas outlet of the neutralization tower (T201) is connected with the gas inlet of the purification tower (T202), the liquid outlet at the bottom of the neutralization tower (T201) is connected with or discharged out of the spray opening at the top of the neutralization tower (T201) through a neutralization tower absorption liquid pump (P204), and the liquid outlet at the bottom of the purification tower (T202) is connected with or discharged out of the spray opening at the top of the purification tower (T202) through a purification tower absorption liquid pump (P205);
the purification vacuum unit comprises a hydrolysis gas-liquid separation tank (V202) and a hydrolysis vacuum unit (P206), wherein a gas inlet of the hydrolysis gas-liquid separation tank (V202) is connected with a gas outlet at the top of a purification tower (T202) in the purification unit, a gas outlet of the hydrolysis gas-liquid separation tank (V202) is connected with the hydrolysis vacuum unit (P206), and a shell pass of the hydrolysis vacuum unit (P206) is connected with external circulating cooling water;
the evaporation concentration unit comprises an evaporator (E201), a separator (S201), a steam saturator (E202), a condenser (E203), a non-condensable gas condenser (E204), a condensate cooler (E205), a concentrated solution cooler (E206), a hot water preheater (E207) and a condensate tank (V203), wherein the shell pass of the evaporator (E201) is connected with the shell pass of the hot water preheater (E207), outside raw steam is discharged or recycled after sequentially passing through the shell pass of the evaporator (E201) and the shell pass of the hot water preheater (E207), a liquid inlet of the hot water preheater (E207) is connected with a shell pass liquid outlet of the concentrated solution cooler (E206), a shell pass liquid inlet of the concentrated solution cooler (E206) is connected with a discharge hole of a hydrolysis kettle in the hydrolysis unit through a hydrolysis discharge pump (P202), and a liquid outlet of the hot water preheater (E207) is connected with a liquid inlet of the separator (S201), a circulating liquid outlet of the separator (S201) is connected with a liquid inlet of an evaporator (E201) through a circulating pump (P207), a liquid outlet of the evaporator (E201) is connected with a circulating liquid inlet of the separator (S201), a liquid outlet of the separator (S201) is connected with a liquid inlet of a concentrated liquid cooler (E206) through a discharge pump (P208), and a liquid outlet of the concentrated liquid cooler (E206) is connected with a finished product sulfuric acid tank; a steam outlet of the separator (S201) is connected with a gas inlet of a steam saturator (E202), a gas outlet of the steam saturator (E202) is connected with a gas inlet of a condenser (E203), and a non-condensable gas outlet of the condenser (E203) is connected with a gas inlet of a non-condensable gas condenser (E204); a condensate outlet of the steam saturator (E202), a condensate outlet of the condenser (E203) and a liquid outlet of the non-condensable gas condenser (E204) are connected with a liquid inlet of a condensate tank (V203), a gas outlet of the condensate tank (V203) is connected with a gas inlet of the condenser (E203), a liquid outlet of the condensate tank (V203) is connected with a liquid inlet of a condensate cooler (E205) through a condensate pump (P209), a liquid outlet of the condensate cooler (E205) is respectively connected with a liquid inlet of a hydrolysis kettle in the hydrolysis unit, a spray port of the steam saturator (E202) and a spray port of the non-condensable gas condenser (E204), and a shell pass of the condenser (E203) and a shell pass of the condensate cooler (E205) are connected with external circulating cooling water;
the evaporation vacuum unit comprises an evaporation gas-liquid separation tank (V204) and a vacuum pump (P210), and a gas outlet of a non-condensable gas condenser (E204) in the evaporation concentration unit is connected with the vacuum pump (P210) through the evaporation gas-liquid separation tank (V204).
2. The device for purification and concentration treatment of nitrosyl sulfuric acid waste liquid according to claim 1, wherein said evaporator (E201), hot water preheater (E207) and condenser (E203) all use high temperature impregnated graphite heat exchangers, said condensate cooler (E205), concentrated liquid cooler (E206) and hydrolysis condenser (E208) all use graphite condensers, and said steam saturator (E202) and non-condensable gas condenser (E204) all use polypropylene materials.
3. The apparatus for purification and concentration treatment of nitrosyl sulfuric acid waste liquid according to claim 2, wherein said hydrolysis kettle is a glass lining reaction kettle; the separator (S201) adopts a steel lining glass lining separator, and the separator (S201) is provided with an independent feed inlet, an observation hole and a liquid level control system for observing and controlling the feed flow.
4. A device for purification and concentration treatment of nitrosyl sulfuric acid waste liquid according to claim 3, wherein said hydrolysis discharge pump (P202), neutralization tower absorption liquid pump (P204), purification tower absorption liquid pump (P205), circulating pump (P207) and discharge pump (P208) are all made of PFA high temperature resistant and corrosion resistant sandwich plate type horizontal pump; the feed pump (P201), the hydrolysis condensate pump (P203) and the condensate pump (P209) are all ultrahigh molecular polyethylene high-temperature-resistant corrosion-resistant leakage-free sandwich type engineering plastic horizontal pumps; the vacuum pump (P210) adopts an LG series dry type constant pitch screw vacuum pump; the hydrolysis vacuum unit (P206) adopts an RPP-280 water injection vacuum unit made of polypropylene.
5. A device for purification and concentration treatment of nitrosyl sulfuric acid waste liquid according to claim 4, wherein, said hydrolysis condensate tank (V201), hydrolysis gas-liquid separation tank (V202), condensate tank (V203) and evaporation gas-liquid separation tank (V204) all adopt polypropylene vertical storage tanks.
6. A device for purification and concentration treatment of nitrosyl sulfuric acid waste liquid according to claim 5, characterized in that said neutralization tower (T201) and purification tower (T202) both adopt HY-II type full negative pressure polypropylene washing tower.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120834404.6U CN214693740U (en) | 2021-04-22 | 2021-04-22 | A device that is used for nitrosyl sulfuric acid waste liquid to purify concentrated processing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120834404.6U CN214693740U (en) | 2021-04-22 | 2021-04-22 | A device that is used for nitrosyl sulfuric acid waste liquid to purify concentrated processing |
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| CN214693740U true CN214693740U (en) | 2021-11-12 |
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| CN202120834404.6U Active CN214693740U (en) | 2021-04-22 | 2021-04-22 | A device that is used for nitrosyl sulfuric acid waste liquid to purify concentrated processing |
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| CN (1) | CN214693740U (en) |
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- 2021-04-22 CN CN202120834404.6U patent/CN214693740U/en active Active
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