CN110160063B - Combustion treatment process for mixed waste acid containing organic matters and heavy metals - Google Patents

Combustion treatment process for mixed waste acid containing organic matters and heavy metals Download PDF

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CN110160063B
CN110160063B CN201810140680.5A CN201810140680A CN110160063B CN 110160063 B CN110160063 B CN 110160063B CN 201810140680 A CN201810140680 A CN 201810140680A CN 110160063 B CN110160063 B CN 110160063B
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acid
valve
condenser
gas
water
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CN110160063A (en
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阮垚
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Ruanshi Chemical Changshu Co ltd
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Ruanshi Chemical Changshu Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048—Purification of waste water by evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N5/00—Systems for controlling combustion
    • F23N5/02—Systems for controlling combustion using devices responsive to thermal changes or to thermal expansion of a medium
    • F23N5/10—Systems for controlling combustion using devices responsive to thermal changes or to thermal expansion of a medium using thermocouples
    • F23N5/102—Systems for controlling combustion using devices responsive to thermal changes or to thermal expansion of a medium using thermocouples using electronic means
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/20—Heavy metals or heavy metal compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/10—Supplementary heating arrangements using auxiliary fuel
    • F23G2204/103—Supplementary heating arrangements using auxiliary fuel gaseous or liquid fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/10—Arrangement of sensing devices
    • F23G2207/101—Arrangement of sensing devices for temperature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/20—Waste supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/30—Oxidant supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/40—Supplementary heat supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N2241/00—Applications
    • F23N2241/18—Incinerating apparatus

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Organic Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • General Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Processing Of Solid Wastes (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

The invention discloses a combustion disposal process for mixed waste acid containing organic matters and heavy metals, which comprises the following steps: the process comprises the steps of configuring a naked fire furnace, arranging a cyclone separator, arranging a heat carrier, arranging a centrifugal separator, arranging a negative pressure fan, arranging a condenser A and a condenser B, starting the negative pressure fan, igniting the naked fire furnace to enable a mist maker to work, opening a compressed gas inlet on the naked fire furnace, opening a delivery pump and a ratio adjusting valve of a waste acid pool, connecting and arranging an air supplementing valve on the compressed air inlet, opening the air supplementing valve, opening a centrifugal separator acid cutting valve, opening an anhydrous metal salt discharge port, recovering pure acid and recovering pure water.

Description

Combustion treatment process for mixed waste acid containing organic matters and heavy metals
Technical Field
The invention relates to a waste acid disposal and utilization technology in the fields of environmental protection and circular economy, in particular to a mixed waste acid combustion treatment process containing both organic matters and heavy metals.
Background
After the reform of the last century is opened, China has developed a huge industrial revolution, China becomes the largest manufacturing country in the world, industrial production is huge, generated industrial wastes are increased, serious pollution to the ecological environment is caused, most of the environmental pollution comes from the wastes of the industrial production, China has given a lot of strict policies for pollution control, a lot of people with environmental defenses are punished, but the punishment is not the purpose, finally pollution control and ecological environment protection are realized, one of difficult and complicated diseases in the field of environmental protection is the treatment of heavy metal organic waste acid, wherein, acid water is difficult to separate, and acid are difficult to separate and recycle, China's mineral industry, metallurgical smelting industry, electronic industry, mechanical manufacturing industry, IT waste acid industry, electroplating industry, chemical industry, millions of tons of metal waste acid is produced at present, thousands of tons of organic waste acid and millions of tons of heavy metals are produced, millions of tons of heavy metal sludge and organic salts are produced in the waste acid treatment process.
The organic metal waste acid is a solution containing organic matters, metal ions, acid and water, the acid in the solution loses the original function, the solution is called waste acid, is corrosive dangerous waste, and is produced in industrial production, such as polishing, electroplating, etching, acid leaching, acid passivation, inorganic metal salt catalysis, inorganic metal salt and other compound reaction and other processes. The metal in the metal waste acid is in an ionic state, and takes heavy metal ions as main components:
such as heavy metals:
copper ion CU+Lead ion Pb+Zinc ion Zn+Ni ion Ni+Titanium ion Co+Antimony ion Sb+Mercury ion Hg+Chromium ion Cd+Bismuth ion Bi+Chromium ion Cr+；
General metals:
sn ion Sn+Iron ion Fe+Aluminum ion Al+；
Noble metal:
gold ion Au+Silver ion Ag+,
Rare earth metals:
lanthanum ion La+Cerium ion Ce+Praseodymium ion Pr+Nd, rubidium ion+
The metal ions are mixed in acid water in a metal salt solution under the action of acid radicals, the boiling point temperature of the metal salt is as high as 1000 ℃, and the acid in the organic heavy metal waste acid is generally strong acid such as hydrochloric acid, sulfuric acid and nitric acid and weak acid such as phosphoric acid and hydrofluoric acid.
The current treatment mode of organic waste acid containing heavy metals is as follows:
the first method is the landfill of heavy metal sludge after neutralization reaction and precipitation, and illegal burial, temporary storage and the like exist, which endangers offspring and endless future affection.
The second mode is dosing treatment, one toxic and harmful substance is dosed, another substance which can not pollute the environment temporarily is generated, heavy metal organic waste acid is treated, people often choose lime, sodium hydroxide and waste acid to generate neutralization reaction, a large amount of sodium salt and calcium salt can be generated by the method, hundreds of millions of tons of sodium salt and calcium salt are discharged into a fresh water system every year in China, mineral substance imbalance of drinking water is caused, and incurable diseases of human are derived;
the third is a biochemical treatment mode, after metal is removed from the heavy metal organic waste acid, aerobic and anaerobic biochemical treatment is carried out by using a biochemical pond, a large amount of bacterial sludge is generated, at present, 80% of the bacterial sludge is effectively buried, 10% of the bacterial sludge is combusted, the remaining 10% of the bacterial sludge is stacked in the open air, the harm is great, and the bacterial sludge effectively buried is a large pollution source after a plurality of years;
the fourth mode is a waste recycling mode, at present, experts in the environmental protection industry generally accept the waste recycling mode, recycling economy is a law for protecting ecological environment, waste is recycled without being discharged, and the treasured of the Jinshan Yinshan under the green water of the Qingshan mountain can be realized.
In the fourth mode, the modes are also various, the heavy metal organic waste acid utilization method is developed to the most advanced ion exchange method charge membrane method and oxidation method from the prior neutralization, roasting, extraction, concentration and crystallization, various methods are discovered through theoretical research and practical application, each method is only one link in the comprehensive utilization process of the heavy metal organic waste acid, the example A, the Letelard company charge membrane method utilizes the principle that positive and negative ions in positive and negative electrodes and waste acid solution are combined with the mutual repulsion and the mutual attraction of the same polarity and the opposite polarity, and cation and anion liquid are respectively isolated and dialyzed in respective bins under the action of an isolating membrane, so that the concentration of acid is continuously improved, water molecules are dialyzed and discharged, the method has a clean production process environment, acid radical ions are soluble ions, the water obtained by dialysis always contains acid, and the charge energy is limited, the acid concentration of the concentrated acid bin is not more than 15 percent, otherwise, the soluble acid radical ions can be subjected to excessive reverse osmosis, so that the visible charge membrane method only dialyzes low-concentration waste acid into acid with concentration of less than 15 percent, the concentration and the concentration are required to be carried out for recycling, the cost of the membrane is high, and the power consumption is high.
Example B, the oxidation process and heavy metal organic waste acid disclosed in tianjin dye eight works react with nitric acid as an oxidant under appropriate conditions to produce dinitroanthraquinone, which is precipitated out to a large extent and crystallized, and concentrated after membrane filtration and suction filtration to obtain acid of a certain concentration for reuse.
Example C, the roasting method disclosed by TAIhacu, australia, is to make waste acid mist, spray lime powder, make acid mist and carbon powder enter the rotary kiln to perform acid-base neutralization reaction simultaneously, and discharge water vapor under the heating action of the rotary kiln to obtain silicate mixture for cement manufacture.
Therefore, the company invents a combustion treatment process for mixed waste acid containing organic matters and heavy metals, breaks through the idea that people cannot pay attention to recycling of waste acid, makes up the defects of the conventional method, and invents a technology for comprehensively utilizing the organic matter heavy metal waste acid by a pyrolysis separation method.
Disclosure of Invention
The invention mainly solves the technical problem of providing a combustion disposal process for mixed waste acid containing organic matters and heavy metals, wherein the organic matters in the waste acid are self-destructed through ignition combustion to generate heat energy, acid radicals and metal ions are thermally decomposed and crystallized by the heat energy to generate anhydrous metal salt solid state recovery, acid mist and water vapor after thermal decomposition and crystallization are input into a centrifugal separator, the acid mist is stripped and condensed to recover gaseous synthetic acid, the residual water vapor is condensed and recovered to ensure that the organic matters are combusted and destroyed, the metal ions are separated from the gaseous state, the synthetic acid is effectively recovered, and the redundant water vapor is recovered to be pure water.
The combustion disposal process of the mixed waste acid containing organic matters and heavy metals comprises the following steps:
the first step is as follows: the open fire furnace is configured, the whole open fire furnace adopts a cylindrical structure, the bottom edge adopts a conical structure, no dead angle gas negative pressure is formed for pumping, no dead angle material sinks, the material in the open fire furnace is selected from ceramic or steel lining ceramic, and a natural gas burner and a compressed gas inlet are arranged on the open fire furnace;
the second step is that: the cyclone separator is arranged, the cyclone separator is cylindrical in shape structure, the bottom of the cyclone separator is of a cone structure, the cyclone separator is made of ceramic or steel-lined ceramic, and the lower ends of the open-fire furnace and the cyclone separator are provided with anhydrous metal salt discharge ports;
the third step: the open fire furnace and the cyclone separator are connected into a whole through a pipeline, and the cyclone separator separates dust generated by the open fire furnace along with acid mist and water vapor through the cyclone separator;
the fourth step: the top of the cyclone separator is connected with a heat carrier, the heat carrier is a vertical tube type heat carrier, the heat carrier is connected with the air outlet of the cyclone separator through a pipeline, quartz glass or zirconia is selected as a material of the heat carrier, a heat carrier gas channel of the heat carrier ensures that gas can smoothly pass through the heat carrier, meanwhile, heat is transferred to metal-containing organic waste acid, and the other end of the heat carrier is connected to the centrifugal separator;
the fifth step: a centrifugal separator is arranged, the centrifugal separator is made of quartz glass or zirconium materials, the centrifugal separators are three groups of centrifugal separators, each centrifugal separator is of a cylindrical structure, three outlets, namely a tangential air inlet, a tangential acid cutting port and a central air outlet, are respectively arranged on the cylindrical structure of the centrifugal separator, the centrifugal container A is arranged at the lower end of a tangent acid cutting opening of the centrifugal separator, the centrifugal container B is arranged at the lower end of a central air outlet of the centrifugal separator, the centrifugal separator is made of glass or steel-lined ceramic, the centrifugal separator is connected with a heat carrier, three ports are arranged according to the gas flow, the gas is ensured to be centrifuged at high speed in the separator to form different acid layers and water layers, different acids and water are cut according to different layers, the condensing area is determined according to the amount of acid generated, and acid gas and water vapor are condensed into liquid state and recovered in the condensers A and B.
According to a preferable technical scheme, the centrifugal separator is arranged in the step, mixed gas is separated at a high speed in an atomization gasification state, a centrifugal layer is formed by mixing gas in a centrifugal container by utilizing acid and the difference between the acid and water density, high-density acid gas is on the inner wall side of the centrifugal container and sinks faster than other low-density gas, then the high-density acid gas is stripped by a cutting opening, so that stripping is performed by one layer, and the stripped acid gas is cooled and absorbed by water to be strippedUnder the condition of controlling the gaseous temperature to be 350-340 ℃, generally arranged from the inner wall, the first layer is SO2, the second layer is NO2, the third layer is HCL, and the fourth layer is water Vapor, fifth layer of hydrofluoric acid . Returning the mixed acid gas to the original centrifugal separation container when the mixed acid gas is stripped in the stripping process, and repeatedly stripping for multiple times to obtain pure single acid and pure water.
And a sixth step: the acid gas and water vapor are introduced into different condensation and recovery devices by two fans with different pressures, so that acid and water separation is realized.
The seventh step: the condenser A and the condenser B are arranged and made of glass or stainless steel, the condenser A and the condenser B are respectively arranged between the negative pressure fan and the centrifugal separator, a pure water buffer tank is arranged at the lower end of the condenser A, and a pure acid buffer tank is arranged at the lower end of the condenser B.
Eighth step: and starting a negative pressure fan to enable each device and the whole set of facilities to form a certain negative pressure, wherein the negative pressure is-800P, and simultaneously starting the condenser A and the condenser B to cool the circulating water facilities, so that the condenser has enough condensed water.
The ninth step: igniting the open fire furnace, and starting the burner so that the temperature of the open fire furnace is slowly increased to between 185 ℃ and 200 ℃. According to a preferable technical scheme, in the step, the combustion process is automatic controllable combustion, wind blowing is adopted, a pilot burner is arranged on a combustor, and natural gas is used as fuel to ignite and raise the temperature of a hearth.
The tenth step: the waste acid pool and the open fire furnace are connected and provided with the mist generator, so that the mist generator works, and atomized waste acid water vapor is combusted in the open fire furnace through material conveying equipment.
The eleventh step: the method comprises the following steps of opening a compressed gas inlet on a naked fire furnace, connecting compressed air equipment through the compressed gas inlet, arranging a control valve on the compressed air equipment, slowly opening a valve to enable a mist generator to have enough compressed air quantity and ensure stable flame to be kept, wherein the ratio of fuel to air is 1:20, the raw waste acid surface area of materials is enlarged by 1000 times through mist generation, the air quantity is supplemented, and air combustion is ensured.
The twelfth step: the waste acid pool is provided with a delivery pump and a ratio regulating valve, the delivery pump and the ratio regulating valve of the waste acid pool are opened, the regulating valve is slowly increased, the input amount of waste acid is ensured, and the temperature in the furnace is ensured to be matched with the load of a burner.
The thirteenth step: the compressed air inlet is connected with an air supplementing valve, the air supplementing valve is opened, and the opening size of the air supplementing valve is determined according to the detection result of the metal-containing organic waste acid content.
According to the working practice, the opening degree of the waste acid is 30% of that of the monosulfuric acid, the opening degree of the waste acid is 40% of that of the mononitric acid, the opening degree of the waste acid is 50% of that of the monohydrochloride, the opening degree of the waste acid is 60% of that of the monohydrofluoride and the opening degree of the mixed acid is 90%.
The fourteenth step is that: setting a centrifugal separator, opening an acid cut-off valve of the centrifugal separator, and according to the detected amount of acid, when the content of the acid is 5%, the opening degree of the cut-off valve of the centrifugal separator is 10%; the acid content is 15%, and the opening degree of a cut-off valve of the centrifugal separator is 25%; the acid content is 25%, the opening degree of the centrifugal separator cut-off valve is 50%, the acid content is 30%, and the opening degree of the centrifugal separator cut-off valve is 85% to 90%.
According to a preferable technical scheme, the combustion value parameter in the step is generally 100-120 ℃ according to the evaporation boiling point of acid water, the set negative pressure air volume is 2 times of the sum of the volume of thermal expansion of materials, the volume of gas and the volume of hot air, when the negative pressure intensity is-10 KPA, the linear speed of solid-gas separation is 18 meters per second, and the gas-state separation rotating flow speed is 25 meters per second.
The fifteenth step: the anhydrous metal salt discharge port is opened, when a certain amount of anhydrous metal products are accumulated in the open-fire furnace combustion material pipe and the cyclone separator, the discharge valve is opened to discharge, and 50% of materials must be taken out in each discharge.
By utilizing the density difference of acid radical metal ions in the aerosol state and the dehydration state, the mixed gas state in the aerosol state rises, and anhydrous metal salt is precipitated.
Sixteenth, step: and pure acid is recovered, a pure acid buffer tank is arranged at the lower end of the condenser B, and when the pure acid liquid level of a certain pure acid buffer tank reaches a certain position, an acid cutting pump is started to send the pure acid to a corresponding storage tank or a storage cubic barrel.
Seventeenth step: and (3) recovering pure water, arranging a pure water buffer tank at the lower end of the condenser A, starting a water cutting pump when the water level in the pure water buffer tank reaches a certain amount, and delivering the pure water to a reuse water pool.
In the eighth step to the seventeenth step, an unmanned operation mode is adopted, a work system of the programmed robot for one shift within 10 hours is selected, and a starting sequence, a shutdown sequence and a fault shutdown sequence are programmed, so that an automatic operation mode is realized.
The shutdown sequence is executed according to a mechanical fault or an online instrument monitoring out-of-control alarm device.
Wherein, the starting sequence is shown in figure 2, the shutdown sequence is shown in figure 3, the fault shutdown sequence is shown in figure 4, the safe operation is ensured, the device is also provided with an oxygen content automatic monitoring on-line instrument, a full-automatic burner, a temperature on-line monitor, a pressure transmitter, a scraper blade measurer, a double silver fork material level on-line instrument, a floating ball type liquid level on-line instrument, a PH on-line instrument and a material conveying on-line ratio regulating valve, the load of a negative pressure fan is controlled by the negative pressure transmitter, once the fan is started, the load of the fan is instructed by the negative pressure transmitter to ensure the negative pressure in the furnace to be-800P, the load of the burner is controlled by a thermocouple temperature sensor to ensure the temperature in the furnace to be 185 ℃ to 200 ℃, a feeding ratio regulating valve of the metal-containing organic waste acid is controlled by the load of the burner, and the, the anhydrous metal salt discharge valve is controlled by a scraper measurer, the discharge valve is opened by a high tuning fork signal, and the discharge valve is closed by a low tuning fork signal.
The facility opening sequence: starting negative pressure air, reaching-800P in 3-5 minutes, starting a combustor, heating to 185 ℃ in 2 hours, starting a compression valve, starting to 100% in 20 minutes, then starting a feeding pump and a ratio valve, reaching the load of the combustor to 100% in 60 minutes, and finally setting independent automatic control of anhydrous metal discharging, independent automatic control of pure acid discharging and automatic liquid level control of pure water discharging.
And (3) closing the feeding ratio valve in the first step, closing the valve for 30 seconds, then closing the compressed air valve, closing the full valve for 30 seconds, closing the combustor, extinguishing fire for 5 minutes, closing the fan, fully stopping the fan for 30 seconds, and finally performing power-off treatment in the last step.
The invention has the beneficial effects that: the invention relates to a combustion treatment process for mixed waste acid containing organic matters and heavy metals, which realizes zero discharge of COD (chemical oxygen demand) by igniting the combustion of the organic matters to destroy the organic matters, utilizes the heat energy of the combustion of the organic matters to recover the pyrolytic acid radical ions and metal ions from crystallized solid products, then separates boiling water vapor and acid mist or pyrolyzed gaseous acid, synthesizes the separated boiling water vapor and the acid mist or the pyrolyzed gaseous acid to generate synthetic acid for recovery, recovers the water vapor into industrial reuse water, realizes the reclamation of the waste acid, changes waste into valuable, and develops ecological development, green development and sustainable development.
Drawings
FIG. 1 is an overall flow chart of a combustion disposal process of mixed waste acid containing organic matters and heavy metals according to the invention;
FIG. 2 is a sequence diagram of an automatically controlled start-up of a combustion disposal process for waste acid containing organic matter, heavy metals and mixed waste acid according to the present invention;
FIG. 3 is a sequence diagram of an automatically controlled shutdown of a combustion disposal process for waste acid containing organic matter, heavy metals, mixed therewith in accordance with the present invention;
FIG. 4 is a sequence diagram of an automatically controlled shutdown of an organic, heavy metal, mixed spent acid combustion disposal process of the present invention;
FIG. 5 is a schematic diagram of the apparatus for burning and disposing mixed waste acid containing organic substances, heavy metals and waste acid according to the present invention;
the parts in the drawings are numbered as follows:
the device comprises a naked flame furnace 1, a natural gas burner 2, a compressed gas inlet 3, a cyclone separator 4, a heat carrier 5, a centrifugal separator 6, a tangential air inlet 601, a tangential acid cutting port 602, a central air outlet 603, an anhydrous metal salt discharge port 604, a centrifugal container A701, a centrifugal container B702, a negative pressure fan 8, a condenser A9, a condenser B10, a waste acid tank 11, a pressure control valve 12, a pure acid buffer tank 13 and a pure water buffer tank 14.
Detailed Description
The following detailed description of the preferred embodiments of the present invention, taken in conjunction with the accompanying drawings, will make the advantages and features of the invention easier to understand by those skilled in the art, and thus will clearly and clearly define the scope of the invention.
Referring to fig. 1 to 5, an embodiment of the present invention includes:
the combustion disposal process for the mixed waste acid containing organic matters and heavy metals has wide application range, is suitable for the production of the mineral industry acid soaking metal process, is suitable for the treatment of the metal solution containing sulfuric acid, is also suitable for the casting industry dilute hydrochloric acid industry, is also suitable for the electronic industry and the circuit board manufacturing industry, is particularly suitable for thoroughly recovering the nitronitrogen, has great difficulty in destroying the waste dilute nitric acid, is difficult to thoroughly eliminate the nitrogen oxides in water if the nitric acid is changed into the nitrate by adding alkali for neutralization, is often combined with the hydrochloric acid and hydrofluoric acid for application in various industries, produces the mixed waste liquid commonly called aqua regia after the mixing application, and does not thoroughly solve the pollution problem of the nitride in recent years by adopting a reverse osmosis membrane concentration method and a tower type rectification method, and uses the nitric acid to generate NO2 and NO gas by pyrolyzing the nitric acid at a certain temperature and supplies enough air, under the gaseous state, NO is changed into NO2, and then water vapor and NO2 are condensed and absorbed in a proper proportion to generate nitric acid with a certain concentration, so that nitrogen oxides are thoroughly recovered, and the problem of total nitrogen pollution is solved.
In summary, the invention relates to a combustion treatment process for mixed waste acid containing organic matters, heavy metals, which comprises the following steps:
the first step is as follows: the open fire furnace is configured, the whole open fire furnace adopts a cylindrical structure, the bottom edge adopts a conical structure, no dead angle gas negative pressure is formed for pumping, no dead angle material sinks, the material in the open fire furnace is selected from ceramic or steel lining ceramic, and a natural gas burner and a compressed gas inlet are arranged on the open fire furnace;
the second step is that: the cyclone separator is arranged, the cyclone separator is cylindrical in shape structure, the bottom of the cyclone separator is of a cone structure, the cyclone separator is made of ceramic or steel-lined ceramic, and the lower ends of the open-fire furnace and the cyclone separator are provided with anhydrous metal salt discharge ports;
the third step: the open fire furnace and the cyclone separator are connected into a whole through a pipeline, and the cyclone separator separates dust generated by the open fire furnace along with acid mist and water vapor through the cyclone separator;
the fourth step: the top of the cyclone separator is connected with a heat carrier, the heat carrier is a vertical tube type heat carrier, the heat carrier is connected with the air outlet of the cyclone separator through a pipeline, quartz glass or zirconia is selected as a material of the heat carrier, a heat carrier gas channel of the heat carrier ensures that gas can smoothly pass through the heat carrier, meanwhile, heat is transferred to metal-containing organic waste acid, and the other end of the heat carrier is connected to the centrifugal separator;
the fifth step: a centrifugal separator is arranged, the centrifugal separator is made of quartz glass or zirconium materials, the centrifugal separators are three groups of centrifugal separators, each centrifugal separator is of a cylindrical structure, three outlets, namely a tangential air inlet, a tangential acid cutting port and a central air outlet, are respectively arranged on the cylindrical structure of the centrifugal separator, the centrifugal container A is arranged at the lower end of a tangent acid cutting opening of the centrifugal separator, the centrifugal container B is arranged at the lower end of a central air outlet of the centrifugal separator, the centrifugal separator is made of glass or steel-lined ceramic, the centrifugal separator is connected with a heat carrier, three ports are arranged according to the gas flow, the gas is ensured to be centrifuged at high speed in the separator to form different acid layers and water layers, different acids and water are cut according to different layers, the condensing area is determined according to the amount of acid generated, and acid gas and water vapor are condensed into liquid state and recovered in the condensers A and B.
According to a preferable technical scheme, the centrifugal separator is arranged in the step, mixed gas is separated at a high speed in an atomization gasification state, acid and acid are utilized, the difference between the acid and the water density is utilized, the gas is mixed in the centrifugal container to form a centrifugal layer, high-density acid gas is arranged on the inner wall side of the centrifugal container and sinks faster than other low-density gas, then the high-density acid gas is stripped by a cutting opening, SO that the stripping is carried out by one layer, the stripped acid gas is cooled and absorbed by water, and the acid gas is generally arranged from the inner wall under the condition that the gas temperature is controlled to be 350-340 ℃, wherein the first layer is SO2, the second layer is NO2, the third layer is HCL, the fourth layer is water vapor, and the fifth layer is hydrofluoric acid. Returning the mixed acid gas to the original centrifugal separation container when the mixed acid gas is stripped in the stripping process, and repeatedly stripping for multiple times to obtain pure single acid and pure water.
And a sixth step: the acid gas and water vapor are introduced into different condensation and recovery devices by two fans with different pressures, so that acid and water separation is realized.
The seventh step: the condenser A and the condenser B are arranged and made of glass or stainless steel, the condenser A and the condenser B are respectively arranged between the negative pressure fan and the centrifugal separator, a pure water buffer tank is arranged at the lower end of the condenser A, and a pure acid buffer tank is arranged at the lower end of the condenser B.
Eighth step: and starting a negative pressure fan to enable each device and the whole set of facilities to form a certain negative pressure, wherein the negative pressure is-800P, and simultaneously starting the condenser A and the condenser B to cool the circulating water facilities, so that the condenser has enough condensed water.
The ninth step: igniting the open fire furnace, and starting the burner so that the temperature of the open fire furnace is slowly increased to between 185 ℃ and 200 ℃. According to a preferable technical scheme, in the step, the combustion process is automatic controllable combustion, wind blowing is adopted, a pilot burner is arranged on a combustor, and natural gas is used as fuel to ignite and raise the temperature of a hearth.
The tenth step: the waste acid pool and the open fire furnace are connected and provided with the mist generator, so that the mist generator works, and atomized waste acid water vapor is combusted in the open fire furnace through material conveying equipment.
The eleventh step: the method comprises the following steps of opening a compressed gas inlet on a naked fire furnace, connecting compressed air equipment through the compressed gas inlet, arranging a control valve on the compressed air equipment, slowly opening a valve to enable a mist generator to have enough compressed air quantity and ensure stable flame to be kept, wherein the ratio of fuel to air is 1:20, the raw waste acid surface area of materials is enlarged by 1000 times through mist generation, the air quantity is supplemented, and air combustion is ensured.
The twelfth step: the waste acid pool is provided with a delivery pump and a ratio regulating valve, the delivery pump and the ratio regulating valve of the waste acid pool are opened, the regulating valve is slowly increased, the input amount of waste acid is ensured, and the temperature in the furnace is ensured to be matched with the load of a burner.
The thirteenth step: the compressed air inlet is connected with an air supplementing valve, the air supplementing valve is opened, and the opening size of the air supplementing valve is determined according to the detection result of the metal-containing organic waste acid content.
According to the working practice, the opening degree of the waste acid is 30% of that of the monosulfuric acid, the opening degree of the waste acid is 40% of that of the mononitric acid, the opening degree of the waste acid is 50% of that of the monohydrochloride, the opening degree of the waste acid is 60% of that of the monohydrofluoride and the opening degree of the mixed acid is 90%.
The fourteenth step is that: setting a centrifugal separator, opening an acid cut-off valve of the centrifugal separator, and according to the detected amount of acid, when the content of the acid is 5%, the opening degree of the cut-off valve of the centrifugal separator is 10%; the acid content is 15%, and the opening degree of a cut-off valve of the centrifugal separator is 25%; the acid content is 25%, the opening degree of the centrifugal separator cut-off valve is 50%, the acid content is 30%, and the opening degree of the centrifugal separator cut-off valve is 85% to 90%.
According to a preferable technical scheme, the combustion value parameter in the step is generally 100-120 ℃ according to the evaporation boiling point of acid water, the set negative pressure air volume is 2 times of the sum of the volume of thermal expansion of materials, the volume of gas and the volume of hot air, when the negative pressure intensity is-10 KPA, the linear speed of solid-gas separation is 18 meters per second, and the gas-state separation rotating flow speed is 25 meters per second.
The fifteenth step: the anhydrous metal salt discharge port is opened, when a certain amount of anhydrous metal products are accumulated in the open-fire furnace combustion material pipe and the cyclone separator, the discharge valve is opened to discharge, and 50% of materials must be taken out in each discharge.
By utilizing the density difference of acid radical metal ions in the aerosol state and the dehydration state, the mixed gas state in the aerosol state rises, and anhydrous metal salt is precipitated.
Sixteenth, step: and pure acid is recovered, a pure acid buffer tank is arranged at the lower end of the condenser B, and when the pure acid liquid level of a certain pure acid buffer tank reaches a certain position, an acid cutting pump is started to send the pure acid to a corresponding storage tank or a storage cubic barrel.
Seventeenth step: and (3) recovering pure water, arranging a pure water buffer tank at the lower end of the condenser A, starting a water cutting pump when the water level in the pure water buffer tank reaches a certain amount, and delivering the pure water to a reuse water pool.
In the eighth step to the seventeenth step, an unmanned operation mode is adopted, a work system of the programmed robot for one shift within 10 hours is selected, and a starting sequence, a shutdown sequence and a fault shutdown sequence are programmed, so that an automatic operation mode is realized.
The shutdown sequence is executed according to a mechanical fault or an online instrument monitoring out-of-control alarm device.
Wherein, the starting sequence is shown in figure 2, the shutdown sequence is shown in figure 3, the fault shutdown sequence is shown in figure 4, the safe operation is ensured, the device is also provided with an oxygen content automatic monitoring on-line instrument, a full-automatic burner, a temperature on-line monitor, a pressure transmitter, a scraper blade measurer, a double silver fork material level on-line instrument, a floating ball type liquid level on-line instrument, a PH on-line instrument and a material conveying on-line ratio regulating valve, the load of a negative pressure fan is controlled by the negative pressure transmitter, once the fan is started, the load of the fan is instructed by the negative pressure transmitter to ensure the negative pressure in the furnace to be-800P, the load of the burner is controlled by a thermocouple temperature sensor to ensure the temperature in the furnace to be 185 ℃ to 200 ℃, a feeding ratio regulating valve of the metal-containing organic waste acid is controlled by the load of the burner, and the, the anhydrous metal salt discharge valve is controlled by a scraper measurer, the discharge valve is opened by a high tuning fork signal, and the discharge valve is closed by a low tuning fork signal.
The facility opening sequence: starting negative pressure air, reaching-800P in 3-5 minutes, starting a combustor, heating to 185 ℃ in 2 hours, starting a compression valve, starting to 100% in 20 minutes, then starting a feeding pump and a ratio valve, reaching the load of the combustor to 100% in 60 minutes, and finally setting independent automatic control of anhydrous metal discharging, independent automatic control of pure acid discharging and automatic liquid level control of pure water discharging.
And (3) closing the feeding ratio valve in the first step, closing the valve for 30 seconds, then closing the compressed air valve, closing the full valve for 30 seconds, closing the combustor, extinguishing fire for 5 minutes, closing the fan, fully stopping the fan for 30 seconds, and finally performing power-off treatment in the last step.
The above description is only an embodiment of the present invention, and not intended to limit the scope of the present invention, and all modifications of equivalent structures and equivalent processes performed by the present specification and drawings, or directly or indirectly applied to other related technical fields, are included in the scope of the present invention.

Claims (5)

1. A combustion treatment process for mixed waste acid containing organic matters and heavy metals is characterized by comprising the following steps: the method comprises the following steps:
the first step is as follows: a naked flame furnace is configured, the whole naked flame furnace adopts a cylindrical structure, the bottom edge of the naked flame furnace adopts a conical structure, the internal material of the naked flame furnace is selected from ceramic or steel lining ceramic, and a natural gas burner and a compressed gas inlet are arranged on the naked flame furnace;
the second step is that: the cyclone separator is arranged, the cyclone separator is cylindrical in shape structure, the bottom of the cyclone separator is of a cone structure, the cyclone separator is made of ceramic or steel-lined ceramic, and the lower ends of the open-fire furnace and the cyclone separator are provided with anhydrous metal salt discharge ports;
the third step: the open fire furnace and the cyclone separator are connected into a whole through a pipeline, and the cyclone separator separates dust generated by the open fire furnace along with acid mist and water vapor through the cyclone separator;
the fourth step: the top of the cyclone separator is connected with a heat carrier, the heat carrier is a vertical tube type heat carrier, the heat carrier is connected with the air outlet of the cyclone separator through a pipeline, quartz glass or zirconia is selected as a material of the heat carrier, a heat carrier gas channel of the heat carrier ensures that gas can smoothly pass through the heat carrier, meanwhile, heat is transferred to metal-containing organic waste acid, and the other end of the heat carrier is connected to the centrifugal separator;
the fifth step: setting a centrifugal separator which is made of quartz glass or zirconium material, wherein the centrifugal separator is three groups of centrifugal separators, each centrifugal separator is of a cylindrical structure, three outlets which are respectively a tangential air inlet, a tangential acid cutting port and a central air outlet are respectively arranged on the cylindrical structure of the centrifugal separator, a centrifugal container A is arranged at the lower end of the tangential acid cutting port of the centrifugal separator, a centrifugal container B is arranged at the lower end of the central air outlet of the centrifugal separator, the centrifugal separator is made of glass or steel-lined ceramic, the centrifugal separator is connected with a heat carrier, the sizes of the three ports are set according to the gas flow, the gas is ensured to be centrifuged at high speed in the centrifugal separator to form different acid layers and water layers, different acids and water are cut out according to different layers, the condensation area is determined according to the generated acid amount, acid gas and water are condensed into liquid state to be recovered in the condenser A and the, the centrifugal separator arranged in the step separates the mixed gas at a high speed in an atomized and gasified state, utilizes the acid and the difference between the acid and the water density to mix the gas in the centrifugal container to form a centrifugal layer, the high-density acid gas is arranged on the inner wall side of the centrifugal container and sinks faster than other low-density gas, and then the high-density acid gas is stripped by using a cut-out, SO that the acid gas obtained by stripping is stripped layer by layer, the stripped acid gas is cooled and absorbed by water, the acid gas is generally arranged from the inner wall under the condition of controlling the gas temperature of 350-340 ℃, the first layer is SO2, the second layer is NO2, the third layer is HCL, the fourth layer is water vapor, the fifth layer is hydrofluoric acid, the mixed acid gas can return to the original centrifugal separation container when being stripped in the stripping process, and the stripping is repeated for a plurality of times to obtain pure single acid and pure water;
and a sixth step: the method comprises the following steps of arranging a negative pressure fan, wherein the negative pressure fan is a sheet type negative pressure fan and is made of a metal material, the negative pressure fan is respectively connected with a condenser A and a condenser B, the condenser A is connected with a centrifugal container A, the condenser B is connected with the centrifugal container B, and acid gas and water gas are introduced into different condensation recovery equipment by using two fans with different pressures so as to realize acid and water separation;
the seventh step: the method comprises the following steps of arranging a condenser A and a condenser B, wherein the condenser A and the condenser B are made of glass or stainless steel, the condenser A and the condenser B are respectively arranged between a negative pressure fan and a centrifugal separator, the lower end of the condenser A is provided with a pure water buffer tank, and the lower end of the condenser B is provided with a pure acid buffer tank;
eighth step: starting a negative pressure fan to enable each device and the whole set of facilities to form a certain negative pressure, wherein the negative pressure is-800P, and simultaneously starting a condenser A and a condenser B to cool a circulating water facility to enable the condenser to have enough condensed water;
the ninth step: igniting the open fire furnace, and starting a burner to slowly raise the temperature of the open fire furnace to between 185 ℃ and 200 ℃;
the tenth step: a mist generator is connected between the waste acid pool and the open fire furnace, so that the mist generator works, and atomized waste acid water vapor is combusted in the open fire furnace through material conveying equipment;
the eleventh step: opening a compressed air inlet on the open fire furnace, connecting compressed air equipment through the compressed air inlet, arranging a control valve on the compressed air equipment, and slowly opening a valve to ensure that the mist generator has enough compressed air, wherein the ratio of fuel to air is 1: 20;
the twelfth step: a delivery pump and a ratio regulating valve are arranged on the waste acid pool, the delivery pump and the ratio regulating valve of the waste acid pool are opened, the regulating valve is slowly increased, the input amount of waste acid is ensured, and the temperature in the furnace is ensured to be matched with the load of a burner;
the thirteenth step: the compressed air inlet is connected with an air supplementing valve, the air supplementing valve is opened, and the opening size of the air supplementing valve is determined according to the detection result of the metal-containing organic waste acid content;
the fourteenth step is that: setting a centrifugal separator, opening an acid cut-off valve of the centrifugal separator, and according to the detected amount of acid, when the content of the acid is 5%, the opening degree of the cut-off valve of the centrifugal separator is 10%; the acid content is 15%, and the opening degree of a cut-off valve of the centrifugal separator is 25%; the acid content is 25%, the opening degree of a cut-out valve of the centrifugal separator is 50%, the acid content is 30%, and the opening degree of a cut-out valve of the centrifugal separator is 85% to 90%;
the fifteenth step: the discharge port of the anhydrous metal salt is opened, when a certain amount of anhydrous metal products are accumulated in the combustion material pipe and the cyclone separator of the open-fire furnace, the discharge valve is opened to discharge, and 50% of materials must be taken out each time of discharging;
sixteenth, step: recovering pure acid, wherein the lower end of the condenser B is provided with a pure acid buffer tank, and when the pure acid liquid level of a certain pure acid buffer tank reaches a certain position, an acid cutting pump is started to send the pure acid to a corresponding storage tank or a storage cubic barrel;
seventeenth step: and (3) recovering pure water, arranging a pure water buffer tank at the lower end of the condenser A, starting a water cutting pump when the water level in the pure water buffer tank reaches a certain amount, and delivering the pure water to a reuse water pool.
2. The process of claim 1, wherein in the ninth step, the combustion process is automatic controllable combustion, wind blowing is adopted, a pilot burner is arranged on the burner, and natural gas is used as fuel to ignite the natural gas to raise the temperature of the hearth.
3. The process of claim 1, wherein in the tenth step, the opening degree of the waste acid is 30% of that of a sulfuric acid air supplement valve, the opening degree of a nitric acid air supplement valve is 40% of that of a hydrochloric acid air supplement valve, the opening degree of the waste acid is 50% of that of a hydrofluoric acid air supplement valve, and the opening degree of a mixed acid air supplement valve is 90%.
4. The process of claim 1, wherein in the eighth step to the seventeenth step, an unmanned operation mode is adopted, a work system of the programmed robot for 10 hours and one shift is selected, a startup sequence, a shutdown sequence and a fault shutdown sequence are programmed, an automatic operation mode is realized, wherein the fault shutdown sequence is prior, and the shutdown sequence is executed according to a mechanical fault or an on-line instrument monitoring out-of-control alarm device.
5. The process of claim 1, wherein the process further comprises an oxygen content automatic monitoring on-line instrument, a full-automatic burner, a temperature on-line monitor, a pressure transmitter, a scraper measurer, a double-silver fork level on-line measuring instrument, a floating ball type liquid level on-line instrument, a pH on-line instrument and a material conveying on-line ratio regulating valve, wherein the load of the negative pressure fan is controlled by the negative pressure transmitter, once the fan is started, the load of the fan is instructed by the negative pressure transmitter to ensure the negative pressure in the furnace to be-800P, the load of the burner is controlled by a thermocouple temperature sensor to ensure the temperature in the furnace to be 185 ℃ to 200 ℃, the metal-containing organic waste acid feeding ratio regulating valve is controlled by the load of the burner, and when the load of the burner reaches a limit, the ratio valve is stopped to be opened, the anhydrous metal salt discharge valve is controlled by a scraper measurer, the discharge valve is opened by a high tuning fork signal, and the discharge valve is closed by a low tuning fork signal.
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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN88103731A (en) * 1987-06-16 1988-12-28 安德烈茨机械制造股份公司 From a kind of metallic acid solution, produce or reclaim the method for this kind acid
US5495063A (en) * 1992-06-29 1996-02-27 Buck Werke Gmbh & Co. Process for environmentally safe destruction of pyrotechnic material
CN1628226A (en) * 2002-02-08 2005-06-15 关口株式会社 Method of incinerating waste liquid utilizing industrial combustion equipment, and mixed liquid
CN101219774A (en) * 2008-01-15 2008-07-16 成都阿斯特克国龙环保工程有限公司 Four-column waste acid regenerating system and technique
CN202494120U (en) * 2011-09-02 2012-10-17 北京航天动力研究所 High N-S based saliferous organic waste liquid incineration and tail gas purification processing system
CN205127631U (en) * 2015-10-26 2016-04-06 河南华唐新材料股份有限公司 Acid mist purification recovery device

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN88103731A (en) * 1987-06-16 1988-12-28 安德烈茨机械制造股份公司 From a kind of metallic acid solution, produce or reclaim the method for this kind acid
US5495063A (en) * 1992-06-29 1996-02-27 Buck Werke Gmbh & Co. Process for environmentally safe destruction of pyrotechnic material
CN1628226A (en) * 2002-02-08 2005-06-15 关口株式会社 Method of incinerating waste liquid utilizing industrial combustion equipment, and mixed liquid
CN101219774A (en) * 2008-01-15 2008-07-16 成都阿斯特克国龙环保工程有限公司 Four-column waste acid regenerating system and technique
CN202494120U (en) * 2011-09-02 2012-10-17 北京航天动力研究所 High N-S based saliferous organic waste liquid incineration and tail gas purification processing system
CN205127631U (en) * 2015-10-26 2016-04-06 河南华唐新材料股份有限公司 Acid mist purification recovery device

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