1. A method for the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash water washing is characterized by comprising the following steps:

obtaining hazardous waste incineration wet deacidification wastewater, and pretreating the hazardous waste incineration wet deacidification wastewater;

carrying out nanofiltration treatment on the pretreated hazardous waste incineration wet deacidification wastewater to obtain sulfate waste liquid and chloride waste liquid;

carrying out evaporation crystallization treatment on the sulfate waste liquid to obtain sulfate crystals;

obtaining fly ash, washing the fly ash to obtain fly ash washing wastewater, and pretreating the fly ash washing wastewater;

carrying out nanofiltration salt separation treatment on the pretreated fly ash washing wastewater to separate calcium salt waste liquid and sodium and potassium salt waste liquid;

carrying out evaporative crystallization and salt separation treatment on the sodium and potassium salt waste liquid to obtain sodium chloride crystals and potassium chloride crystals;

and synthesizing gypsum by using the chlorine salt waste liquid and the calcium salt waste liquid, and obtaining a sodium chloride solution.

2. The method of claim 1, wherein the synthesizing gypsum from the chlorine salt waste liquid and the calcium salt waste liquid and obtaining a sodium chloride solution comprises:

adding the chlorine salt waste liquid and the calcium salt waste liquid into a gypsum synthesis kettle, and reacting sulfate radicals in the chlorine salt waste liquid with calcium ions in the calcium salt waste liquid to generate calcium sulfate crystals;

adding the waste liquid in the gypsum synthesis kettle into a gypsum crystallization kettle for reaction so as to grow the calcium sulfate crystals;

and carrying out centrifugal separation on the waste liquid in the gypsum crystallization kettle to obtain the calcium sulfate gypsum.

3. The method of claim 2, further comprising:

softening and decalcifying the waste liquid obtained by centrifugal separation to obtain the sodium chloride solution, and carrying out evaporation crystallization and salt separation treatment on the sodium chloride solution and the sodium and potassium salt waste liquid.

4. The method of claim 2 wherein the chlorine salt waste liquid and the calcium salt waste liquid are fed into the gypsum synthesis kettle in a counter-current manner.

5. The method of claim 2, wherein the residence time of the waste stream in the gypsum synthesis kettle and the gypsum crystallization kettle is 2-12 hours.

6. The method of claim 2, wherein the gypsum synthesis kettle is provided with a first overflow port through which waste liquid in the gypsum synthesis kettle flows automatically to the gypsum crystallization kettle.

7. The method of claim 6, wherein the gypsum crystallization kettle is provided with a second overflow port, and calcium sulfate crystals in the upper layer of the waste liquid are returned to the gypsum synthesis kettle from the second overflow port during stirring of the waste liquid in the gypsum crystallization kettle.

8. The method of claim 1, further comprising:

when the water yield of the chlorine salt waste liquid is insufficient, replacing the chlorine salt waste liquid with the hazardous waste incineration wet deacidification waste water to synthesize gypsum;

and when the water yield of the calcium salt waste liquid is insufficient, replacing the calcium salt waste liquid with the fly ash water washing waste water to synthesize gypsum.

9. The utility model provides a system that danger is useless to burn wet process deacidification and is dealt with flying dust washing in coordination, its characterized in that, the system includes:

the hazardous waste incineration wet deacidification wastewater pretreatment device is used for obtaining hazardous waste incineration wet deacidification wastewater and pretreating the hazardous waste incineration wet deacidification wastewater;

the nanofiltration device is used for carrying out nanofiltration treatment on the pretreated hazardous waste incineration wet deacidification wastewater to obtain sulfate waste liquid and chloride waste liquid;

the evaporative crystallization device is used for carrying out evaporative crystallization treatment on the sulfate waste liquid to obtain sulfate crystals;

the fly ash washing device is used for washing fly ash to obtain fly ash washing wastewater;

the fly ash washing wastewater pretreatment device is used for pretreating the fly ash washing wastewater;

the nano-filtration salt separation device is used for carrying out nano-filtration salt separation treatment on the pretreated fly ash washing wastewater so as to separate calcium salt waste liquid and sodium potassium salt waste liquid;

the evaporative crystallization salt separation device is used for carrying out evaporative crystallization salt separation treatment on the sodium potassium salt waste liquid to obtain sodium chloride crystals and potassium chloride crystals;

and the gypsum synthesis device is used for synthesizing gypsum by using the chlorine salt waste liquid and the calcium salt waste liquid and obtaining a sodium chloride solution.

10. The system of claim 9, wherein the gypsum synthesis apparatus comprises:

the gypsum synthesis kettle is used for obtaining the chlorine salt waste liquid and the calcium salt waste liquid, so that sulfate radicals in the chlorine salt waste liquid and calcium ions in the calcium salt waste liquid react to generate calcium sulfate crystals;

the gypsum crystallization kettle is used for obtaining waste liquid in the gypsum synthesis kettle and growing the calcium sulfate crystals;

and the centrifugal device is used for carrying out centrifugal separation on the waste liquid in the gypsum crystallization kettle to obtain the gypsum.

Background

In recent years, waste incineration has become a mainstream trend of domestic waste treatment due to its advantages of reduction, harmlessness, and recycling. In the process of burning garbage, a large amount of fly ash is generated, the fly ash is rich in high-concentration chlorine salt (mainly taking the chlorine salt of Na, K and Ca) and also contains certain harmful components such as dioxin, heavy metal and the like, and the fly ash belongs to dangerous waste. Therefore, the fly ash must be strictly disposed before landfill and resource utilization, and the current method for doping the waste incineration fly ash into cement after washing is an effective method for resource utilization of the waste incineration fly ash. The chlorine salt is leached out when the fly ash is washed by water, a large amount of high-salt wastewater is generated, and the wastewater contains higher-concentration chloride ions and calcium ions, so that the hardness of the water reaches over 20000mg/L, and meanwhile, lead, chromium, cadmium, copper, zinc, nickel and other heavy metals can also partially enter the solution. Therefore, the research on the feasible technology of the fly ash washing wastewater treatment is urgent.

On the other hand, because wet deacidification efficiency is higher, it is comparatively extensive to use in the treatment of the waste incineration flue gas, and wet tower deacidification waste water is mainly the drainage of absorption tower in the deacidification process. The impurities contained in the deacidification wastewater mainly comprise suspended matters, sulfate, chloride and a small amount of heavy metals, wherein a lot of the impurities are pollutants which are strictly controlled in the environmental protection standard, and how to effectively and economically treat the wet-process deacidification wastewater is of great significance.

Disclosure of Invention

In this summary, concepts in a simplified form are introduced that are further described in the detailed description. This summary of the invention is not intended to identify key features or essential features of the claimed subject matter, nor is it intended to be used as an aid in determining the scope of the claimed subject matter.

Aiming at the defects of the prior art, the invention provides a method for the cooperative treatment of the wet deacidification of hazardous waste incineration and the washing of fly ash, which comprises the following steps:

obtaining hazardous waste incineration wet deacidification wastewater, and pretreating the hazardous waste incineration wet deacidification wastewater;

carrying out nanofiltration treatment on the pretreated hazardous waste incineration wet deacidification wastewater to obtain sulfate waste liquid and chloride waste liquid;

carrying out evaporation crystallization treatment on the sulfate waste liquid to obtain sulfate crystals;

obtaining fly ash, washing the fly ash to obtain fly ash washing wastewater, and pretreating the fly ash washing wastewater;

carrying out nanofiltration salt separation treatment on the pretreated fly ash washing wastewater to separate calcium salt waste liquid and sodium and potassium salt waste liquid;

carrying out evaporative crystallization and salt separation treatment on the sodium and potassium salt waste liquid to obtain sodium chloride crystals and potassium chloride crystals;

and synthesizing gypsum by using the chlorine salt waste liquid and the calcium salt waste liquid, and obtaining a sodium chloride solution.

In one embodiment, the synthesizing gypsum by using the chlorine salt waste liquid and the calcium salt waste liquid and obtaining a sodium chloride solution comprises:

adding the chlorine salt waste liquid and the calcium salt waste liquid into a gypsum synthesis kettle, and reacting sulfate radicals in the chlorine salt waste liquid with calcium ions in the calcium salt waste liquid to generate calcium sulfate crystals;

adding the waste liquid in the gypsum synthesis kettle into a gypsum crystallization kettle for reaction so as to grow the calcium sulfate crystals;

and carrying out centrifugal separation on the materials in the gypsum crystallization kettle to obtain the gypsum.

In one embodiment, the method further comprises:

softening and decalcifying the waste liquid obtained by centrifugal separation to obtain a sodium chloride solution, and carrying out evaporation crystallization and salt separation treatment on the sodium chloride solution and the sodium and potassium salt waste liquid.

In one embodiment, the chlorine salt waste liquid and the calcium salt waste liquid enter the gypsum synthesis kettle in a convection feeding mode.

In one embodiment, the residence time of the waste stream in the gypsum synthesis kettle and the gypsum crystallization kettle is between 2 and 12 hours.

In one embodiment, the gypsum synthesis kettle is provided with a first overflow port, and waste liquid in the gypsum synthesis kettle automatically flows to the gypsum crystallization kettle through the first overflow port.

In one embodiment, the gypsum crystallization kettle is provided with a second overflow port, and calcium sulfate crystals on the upper layer of the waste liquid are returned to the gypsum synthesis kettle from the second overflow port in the process of stirring the waste liquid in the gypsum crystallization kettle.

In one embodiment, the method further comprises:

when the water yield of the chlorine salt waste liquid is insufficient, replacing the chlorine salt waste liquid with the hazardous waste incineration wet deacidification waste water to synthesize gypsum;

and when the water yield of the calcium salt waste liquid is insufficient, replacing the calcium salt waste liquid with the fly ash water washing waste water to synthesize gypsum.

In another aspect, an embodiment of the present invention provides a system for performing cooperative disposal of hazardous waste incineration wet deacidification and fly ash washing, where the system includes:

the hazardous waste incineration wet deacidification wastewater pretreatment device is used for obtaining hazardous waste incineration wet deacidification wastewater and pretreating the hazardous waste incineration wet deacidification wastewater;

the nanofiltration device is used for carrying out nanofiltration treatment on the pretreated hazardous waste incineration wet deacidification wastewater to obtain sulfate waste liquid and chloride waste liquid;

the evaporative crystallization device is used for carrying out evaporative crystallization treatment on the sulfate waste liquid to obtain sulfate crystals;

the fly ash washing device is used for washing fly ash to obtain fly ash washing wastewater;

the fly ash washing wastewater pretreatment device is used for pretreating fly ash washing wastewater;

the nano-filtration salt separation device is used for carrying out nano-filtration salt separation treatment on the pretreated fly ash washing wastewater so as to separate calcium salt waste liquid and sodium potassium salt waste liquid;

the evaporative crystallization salt separation device is used for carrying out evaporative crystallization salt separation treatment on the sodium potassium salt waste liquid to obtain sodium chloride crystals and potassium chloride crystals;

and the gypsum synthesis device is used for synthesizing gypsum by using the chlorine salt waste liquid and the calcium salt waste liquid and obtaining a sodium chloride solution.

In one embodiment, the gypsum synthesis apparatus comprises:

the gypsum synthesis kettle is used for obtaining the chlorine salt waste liquid and the calcium salt waste liquid, so that sulfate radicals in the chlorine salt waste liquid and calcium salts in the calcium salt waste liquid react to generate calcium sulfate crystals;

the gypsum crystallization kettle is used for obtaining waste liquid in the gypsum synthesis kettle and growing the calcium sulfate crystals;

and the centrifugal device is used for carrying out centrifugal separation on the waste liquid in the gypsum crystallization kettle to obtain gypsum.

The method and the system for the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash water washing provided by the invention perform the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash water washing, thereby realizing the comprehensive recycling of the high-salinity waste liquid.

Drawings

The following drawings of the invention are included to provide a further understanding of the invention. The drawings illustrate embodiments of the invention and, together with the description, serve to explain the principles of the invention.

In the drawings:

FIG. 1 is a flow chart of a method for co-processing hazardous waste incineration wet deacidification and fly ash washing according to an embodiment of the invention;

FIG. 2 is a schematic structural diagram of a hazardous waste incineration wet deacidification waste liquid treatment unit in a hazardous waste incineration wet deacidification and fly ash water washing co-processing system according to an embodiment of the present invention;

FIG. 3 is a schematic structural diagram of a fly ash water washing wastewater treatment unit in a system for hazardous waste incineration wet deacidification and fly ash water washing cooperative treatment according to an embodiment of the present invention;

fig. 4 is a schematic structural diagram of a gypsum synthesis unit in a system for the co-disposal of hazardous waste incineration wet deacidification and fly ash washing according to one embodiment of the present invention.

Detailed Description

In the following description, numerous specific details are set forth in order to provide a more thorough understanding of the present invention. It will be apparent, however, to one skilled in the art, that the present invention may be practiced without one or more of these specific details. In other instances, well-known features have not been described in order to avoid obscuring the invention.

In the following description, specific method steps and/or structures are set forth in order to provide a thorough understanding of the present invention. It will be apparent that the invention may be practiced without limitation to the specific details known to those skilled in the art. The following detailed description of the preferred embodiments of the invention, however, the invention is capable of other embodiments in addition to those detailed.

It is to be understood that the present invention may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art. In the drawings, the size and relative sizes of layers and regions may be exaggerated for clarity. Like reference numerals refer to like elements throughout.

It will be understood that the terms "comprises" and/or "comprising," when used in this specification, specify the presence of stated features, integers, steps, operations, elements, and/or components, but do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof. The singular forms "a", "an" and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.

The treatment process of the hazardous waste incineration wet deacidification wastewater and the fly ash washing wastewater mainly relates to two stages of pretreatment and advanced treatment. The pretreatment mainly uses a chemical method to remove F in wastewater^-、Ca²⁺、Mg²⁺And part of heavy metal ions, and the advanced treatment is used for removing salt in the wastewater and crystallizing out the salt for recycling. The pretreatment stage is mainly to add special flocculating agent, antisludging agent, softening agent and the like into the sulfur wastewater to ensure that calcium, heavy metal ions and the like in the wastewater and the medicament form precipitates which are stripped from the water, thereby realizing the purpose of removal. However, the wastewater treatment method has the problems of large dosage of medicament, high cost, generation of a large amount of sludge, secondary pollution and the like; meanwhile, new substances are introduced, new impurity ions are generated in water, and new problems are brought to subsequent treatment.

The deep treatment stage mainly utilizes a film technology and an evaporation salt separation crystallization technology, and after pretreatment is carried out through the film technology, evaporation salt separation crystallization is further carried out, and a multi-effect evaporator is generally adopted for evaporation salt separation. At present, nanofiltration is widely used for separating high-valence salt from low-valence salt, but a membrane has certain selectivity on the interception of ions, the interception rate of calcium and magnesium can reach 98%, and the interception rate of sulfate radicals is generally only about 80%, so that on the basis of nanofiltration membrane treatment, the waste water recycling of sulfate is realized, and an evaporation salt separation crystallization technology is also required to be combined. At present, the multi-effect evaporator has mature technology and wide application range, can reduce partial energy consumption, but when the waste water contains miscellaneous salts, the saline water has strong corrosivity at high temperature, and has higher requirements on the equipment and material selection of the multi-effect evaporator, thereby causing the increase of equipment cost and further causing the high construction investment cost; in the evaporation salt separation crystallization operation process, different evaporation temperatures and waste liquid concentrations need to be controlled to separate salt, a large amount of electric energy and water vapor are consumed, and the operation cost is high.

In some existing wet desulfurization wastewater treatment processes, fly ash and desulfurization wastewater are mixed to form wet fly ash, pollutants in the desulfurization wastewater are adsorbed, boiler flue gas is used for drying the wet fly ash and then enters a dust remover, but chlorine in the desulfurization wastewater volatilizes into the flue gas and corrodes a flue and a subsequent flue gas purification device; and the subsequent treatment of the wastewater is not mentioned, and the salt is not recycled.

Ca in fly ash is contained if only by uniformly mixing the refuse incineration fly ash with the desulfurization waste water²⁺With SO in the desulfurization waste water₄ ^2-Combine to form CaSO₄Further solidifying the heavy metal in the fly ash, absorbing the heavy metal and impurities in the desulfurization waste water by the porous structure of the fly ash, simultaneously enriching the chlorine in the waste incineration fly ash in the desulfurization waste water, but enriching the SO in the desulfurization waste water₄ ^2-The concentration of (2) limits the solidification capability of the heavy metals, and the chlorine enriched in the desulfurization wastewater is difficult to be properly treated subsequently, and the salt separation and resource utilization of the salt cannot be realized.

If hydrothermal conditions are used as a treatment environment, the fly ash and the wastewater are subjected to hydrothermal reaction, so that the fly ash has strong adsorption capacity on heavy metals, and the heavy metals in the wastewater can be transferred to the fly ash and exist in a stable and difficult-to-desorb form.

If the fly ash and the desulfurization wastewater are mixed and stirred and extracting agents such as phosphoric acid and the like are added, the pH of the desulfurization wastewater is adjusted, heavy metals in a cation form in the desulfurization wastewater are adsorbed, and heavy metals in an anion form in the fly ash are effectively removed, so that harmless and recycling treatment of the fly ash can be correspondingly realized.

In summary, the prior art mainly aims at the treatment of desulfurization (limestone/gypsum method) wastewater and fly ash, but does not perform cooperative treatment on a hazardous waste incineration system and fly ash, and meanwhile, the existing treatment process cannot well realize comprehensive recycling of salt, and the pretreatment and advanced treatment stages have some defects in the application process. Therefore, aiming at the water quality characteristics of the two types of waste water, namely the hazardous waste incineration wet deacidification waste water and the fly ash washing waste water, a novel method and a novel system for the cooperative treatment of the waste water are explored and developed, comprehensive recycling is realized, and the method and the system have important significance.

Based on the method and the system, the embodiment of the invention provides a method and a system for the cooperative treatment of the hazardous waste incineration wet deacidification and the fly ash water washing, most of soluble salt is washed into the solution by the fly ash water washing, and the washed fly ash reaches the landfill standard and enters a landfill site or is recycled outside; after impurities such as heavy metals, suspended matters and the like are removed from the fly ash washing wastewater by a pretreatment device, the fly ash washing wastewater enters a nanofiltration salt separation system to realize the separation of calcium ions from sodium and potassium, and high-calcium waste liquid is obtained; after pretreatment, the hazardous waste incineration wet deacidification wastewater enters a nanofiltration device to obtain high-chlorine sulfate-containing waste liquid, and the high-chlorine sulfate-containing waste liquid is combined with the high-calcium waste liquid to synthesize gypsum, so that sulfate radicals in the high-chlorine waste water are effectively utilized; and finally, returning the high-purity sodium chloride solution to the fly ash washing process for salt separation and crystallization to realize resource recovery.

In order to provide a thorough understanding of the present invention, a detailed structure will be set forth in the following description in order to explain the present invention. The following detailed description of the preferred embodiments of the invention, however, the invention is capable of other embodiments in addition to those detailed.

The method for the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash water washing according to the embodiment of the invention is further described with reference to fig. 1. The hazardous waste incineration wet deacidification and fly ash water washing cooperative treatment of the embodiment of the invention mainly comprises the treatment of hazardous waste incineration wet deacidification wastewater, the treatment of fly ash water washing wastewater and the cooperative treatment of the hazardous waste incineration wet deacidification wastewater and the fly ash water washing wastewater to synthesize gypsum.

As shown in fig. 1, aiming at the treatment of the deacidification wastewater by the hazardous waste incineration application method, firstly, the deacidification wastewater by the hazardous waste incineration wet method is obtained, and the deacidification wastewater by the hazardous waste incineration wet method is pretreated. The pretreatment is mainly used for removing impurities in the hazardous waste incineration wet deacidification wastewater. Then, carrying out nanofiltration treatment on the pretreated hazardous waste incineration wet deacidification wastewater to obtain sulfate waste liquid and chloride waste liquid; and (3) carrying out evaporation crystallization treatment on the sulfate waste liquid to obtain a sulfate crystal product, wherein the obtained sulfate crystal product can be sold for the outside, and the chloride waste liquid still contains certain sulfate radicals for subsequent gypsum synthesis.

For example, referring to fig. 2, after the hazardous waste incineration wet deacidification wastewater is pumped from the raw water storage tank 1 to the hazardous waste incineration wet deacidification wastewater pretreatment device 2, the hazardous waste incineration wet deacidification wastewater enters the nanofiltration device 3 through the high-pressure pump, so that the sulfate waste liquid and the chloride waste liquid are separated and stored in the chloride water production storage tank 4 and the sulfate water production storage tank 5 respectively. The sulfate waste liquid can obtain a sodium sulfate crystallization product after passing through the evaporation crystallization device 6, the evaporation mother liquid is temporarily stored in the first evaporation mother liquid storage tank 7 and returns to the evaporation system, and when the chlorine salt is enriched to a certain concentration, the chlorine salt returns to the nanofiltration device 3 for treatment.

On the other hand, for the fly ash washing, fly ash is first obtained, the fly ash is washed to obtain fly ash washing wastewater, and the fly ash washing wastewater is pretreated. Most of the soluble salt is washed into the solution by washing the fly ash, and the washed fly ash reaches the landfill standard and enters a landfill site or is used as a cement raw material for recycling. The pretreatment of the fly ash washing wastewater is mainly used for removing impurities such as heavy metals, suspended matters and the like. And then, carrying out nanofiltration salt separation treatment on the pretreated fly ash washing wastewater to separate calcium salt waste liquid and sodium and potassium salt waste liquid. And carrying out evaporative crystallization and salt separation treatment on the sodium and potassium salt waste liquid to obtain sodium chloride crystals and potassium chloride crystals. Among them, sodium chloride crystals and potassium chloride crystals are available for sale, and calcium salts are used for the subsequent synthesis of gypsum.

Illustratively, referring to fig. 3, the fly ash is washed by a fly ash washing device 8, the washed fly ash is transported to landfill or outsourcing for recycling, the washing waste liquid is pretreated by a fly ash washing waste water pretreatment device and filtered by a bag filter, the water washing waste liquid is treated by a high-pressure pump to enter a nanofiltration salt separating device 9, the nanofiltration salt separating device 9 separates calcium salt from sodium salt and potassium salt in the water washing waste liquid, the obtained calcium salt waste liquid and the sodium salt and potassium salt waste liquid are respectively stored in a calcium salt water production storage tank 10 and a sodium salt and potassium salt water production storage tank 11, the sodium salt and potassium salt waste liquid enters an evaporative crystallization salt separating device 12, sodium chloride crystals and potassium chloride crystals are respectively obtained after evaporation crystallization salt separation, an evaporative mother liquid is temporarily stored in a second evaporative mother liquid storage tank 13, the evaporative crystallization salt separating device 12 returns to continue salt separation crystallization, and when calcium ions are enriched to a certain extent, the calcium ions are returned to the nanofiltration salt separating device 9 to be treated to remove the calcium ions.

Therefore, the treatment of the hazardous waste incineration deacidification wastewater is performed to obtain the chloride waste liquid containing sulfate radicals, the treatment of the fly ash washing wastewater is performed to obtain the calcium salt waste liquid, then sulfate ions in the chloride waste liquid and calcium ions in the calcium salt waste liquid can be utilized to synthesize calcium sulfate gypsum, and meanwhile, the sodium chloride solution is obtained, so that the salt in the high-salt waste water can be fully utilized.

Further, the synthesis of the calcium sulfate gypsum by using sulfate ions in the chlorine salt waste liquid and calcium ions in the calcium salt waste liquid comprises the following steps: adding the waste chlorine salt solution and the waste calcium salt solution into a gypsum synthesis kettle, and reacting sulfate radicals in the waste chlorine salt solution with calcium ions in the waste calcium salt solution to generate calcium sulfate crystals; adding waste liquid in a gypsum synthesis kettle into a gypsum crystallization kettle for reaction so as to grow calcium sulfate crystals; and carrying out centrifugal separation on the waste liquid in the gypsum crystallization kettle to obtain the calcium sulfate gypsum.

And simultaneously, softening and decalcifying the waste liquid obtained by centrifugal separation to obtain a sodium chloride solution, and carrying out evaporative crystallization and salt separation treatment on the sodium chloride solution and the sodium and potassium salt waste liquid together to obtain a sodium chloride crystal product.

Referring to fig. 4, the chlorine salt waste liquid and the calcium salt waste liquid enter the gypsum synthesis kettle 14 in a convection feeding manner. Respectively controlling the feeding flow rates of the chlorine salt waste liquid and the calcium salt waste liquid, and respectively feeding the chlorine salt waste liquid and the calcium salt waste liquid into the gypsum synthesis kettle 14 in a convection manner to react residual sulfate radicals/sodium sulfate in the chlorine salt waste liquid with calcium salt to synthesize calcium sulfate gypsum and sodium chloride, wherein the feeding speed is, for example, m (Ca) m (SO)₄) 1.0-1.2. The gypsum synthesis kettle 14 is provided with a first overflow port, and waste liquid in the gypsum synthesis kettle 14 flows to the gypsum crystallization kettle 15 through the first overflow port automatically, further complete reaction is carried out at the position, longer retention time is guaranteed simultaneously, calcium sulfate crystals grow up, solid-liquid separation is facilitated, and product quality is improved. The gypsum crystallization kettle 15 is provided withAnd the second overflow port is used for returning calcium sulfate crystals on the upper layer of the waste liquid to the gypsum synthesis kettle 14 from the second overflow port in the process of stirring the waste liquid in the gypsum crystallization kettle 15. And (3) centrifugally separating the waste liquid in the gypsum crystallization kettle 15 to obtain a gypsum product, softening and decalcifying the waste liquid obtained after centrifugal separation by using a deep decalcification reaction device 16 to obtain a sodium chloride refined liquid, and returning the refined liquid to the evaporative crystallization salt separation device 12 for salt separation to obtain sodium chloride. In one embodiment, the residence time of the waste stream in the gypsum synthesis kettle 14 and the gypsum crystallization kettle 15 is 2-12 hours to ensure that the waste stream is fully reacted.

In one embodiment, when the water yield of the chlorine salt waste liquid is insufficient, the hazardous waste incineration wet deacidification waste water or sodium sulfate is used for replacing the chlorine salt waste liquid to synthesize gypsum; when the water yield of the calcium salt waste liquid is insufficient, the fly ash washing waste water replaces the calcium salt waste liquid to synthesize the gypsum.

According to the embodiment of the invention, different nanofiltration treatments are used for separating high-valent ion calcium and the like and low-valent ion sodium and potassium in the fly ash washing wastewater and separating high-valent ion sulfate radicals and the low-valent ion chloride ions in the hazardous waste incineration wet deacidification wastewater, meanwhile, the high-calcium waste liquid and the high-chlorine sulfate radical containing waste liquid are cooperated to synthesize gypsum, and the obtained high-purity sodium chloride solution is returned to be recycled, so that the comprehensive recycling of salt in the waste liquid is finally realized. The embodiment of the invention does not introduce impurities outside the system, saves cost, is environment-friendly, realizes comprehensive recycling of the high-salt waste liquid, and is suitable for recycling of the high-salt waste liquid in industries such as hazardous waste and the like.

According to the embodiment of the invention, nanofiltration membrane technology is adopted, nanofiltration water is innovatively used to synergistically co-produce calcium sulfate gypsum and sodium chloride, meanwhile, crystallization technology is applied to the production process to obtain high-quality gypsum, and finally, through the desalination crystallization technology, synergistic treatment of hazardous waste incineration wet deacidification wastewater and fly ash washing wastewater is realized, and comprehensive recycling is realized. By using a nanofiltration technology, calcium ions in the fly ash washing wastewater can be effectively separated from potassium and sodium ions, most sulfate radicals and chloride ions in the hazardous waste incineration wet deacidification wastewater can also be separated, the fly ash washing wastewater is changed into a potassium and sodium binary system from high-salt wastewater of a calcium, potassium and sodium ternary system, the deacidification wastewater is changed into high-purity sodium sulfate wastewater, the subsequent salt separation crystallization process flow is simplified, the evaporation cost and the power consumption are reduced, and the quality of a crystallization product is greatly improved. Because the hazardous waste incineration wet deacidification wastewater is mainly high-concentration sulfate, a certain amount of sulfate and chloride penetrate through the nanofiltration membrane to enter into the chloride production water, the sulfate radical in the chloride production water reacts with calcium chloride in the calcium salt water-washing calcium salt production water of fly ash, and meanwhile, high-quality calcium sulfate gypsum is obtained by controlling the reaction speed and the crystallization process of synthesis; after softening and decalcifying the sodium chloride, returning the sodium chloride to the fly ash washing device to co-produce a sodium chloride crystal product; on the basis of the former stage treatment, the salt separation crystallization technology is utilized to obtain high-quality sodium chloride, potassium chloride and sodium sulfate products, and comprehensive recycling is realized. The method is environment-friendly, no external impurities are introduced, two kinds of wastewater are treated cooperatively in the treatment process, the treatment cost is greatly reduced, and the product quality is high, so that the method is suitable for large-scale engineering production and application.

Example 1

Taking the first hazardous waste incineration wet deacidification wastewater as a raw material, pretreating the first hazardous waste incineration wet deacidification wastewater, then feeding the pretreated hazardous waste incineration wet deacidification wastewater into a nanofiltration device to realize primary salt separation, and feeding the obtained high-purity sulfate waste liquid into an evaporation crystallization salt separation device to obtain a sodium sulfate product; the method comprises the following steps that firstly, waste incineration fly ash enters a fly ash washing device, soluble salts such as chloride and the like enter a solution, the solution is pretreated and then enters a nanofiltration device to realize primary salt separation, and the obtained sodium and potassium solution wastewater enters an evaporation crystallization salt separation device to obtain potassium chloride and sodium chloride products; and (4) the chlorine salt produced water obtained by nanofiltration and the calcium salt are produced and enter a gypsum synthesis device, and finally gypsum and sodium chloride are co-produced, so that comprehensive recycling is realized.

The method comprises the following specific steps:

pumping the hazardous waste incineration wet deacidification wastewater from a raw water storage tank to a pretreatment device, then pumping the hazardous waste incineration wet deacidification wastewater into a sulfate nanofiltration device through a high-pressure pump, separating sulfate and chloride and storing the sulfate and the chloride in a chloride generation storage tank and a sulfate storage tank respectively, obtaining a sodium sulfate crystallization product I (the main components are shown in table 1) after the sulfate waste liquid passes through an evaporation crystallization system, temporarily storing the evaporation mother liquid in the evaporation mother liquid storage tank, returning the evaporation mother liquid to the evaporation system, and returning the evaporation mother liquid to the nanofiltration device for treatment when the chloride is enriched to a certain concentration; fly ash washing deviceAfter washing, conveying the fly ash to landfill or outsourcing recycling, pretreating washing waste liquid, then feeding the pretreated washing waste liquid into a nanofiltration salt separation device by using a high-pressure pump, separating calcium salt, sodium salt and potassium salt, and then respectively storing the calcium salt, the sodium salt and the potassium salt in a calcium salt water production storage tank and a sodium salt and potassium salt water production storage tank, respectively obtaining a sodium chloride crystal product I (the main components are shown in a table 2) and a potassium chloride crystal product I (the main components are shown in a table 3) from the sodium salt and potassium salt waste liquid by an evaporation crystallization salt separation device, temporarily storing the evaporation mother liquid in an evaporation mother liquid storage tank, returning the evaporation crystallization salt separation device to continue salt separation and crystallization, and when calcium ions are enriched to a certain extent, returning the evaporation crystallization salt separation device to treat and remove calcium ions; respectively controlling the feeding flow rates of the chlorine salt waste liquid and the calcium salt waste liquid, and respectively feeding the chlorine salt waste liquid and the calcium salt waste liquid into a gypsum synthesis kettle in a convection manner, wherein the feeding speeds of the chlorine salt waste liquid and the calcium salt waste liquid are controlled to be m (Ca) m (SO)₄) 1.0, controlling the residence time of the solution in a gypsum synthesis kettle and a gypsum crystallization kettle to be 2 hours, reacting residual sulfate radicals/sodium sulfate in chloride with calcium salt to synthesize calcium sulfate gypsum and sodium chloride, automatically flowing the synthesized slurry to the gypsum crystallization kettle through an overflow port, further completely reacting, ensuring longer residence time of synthesized particles, growing calcium sulfate crystals, being more beneficial to solid-liquid separation and improving the product quality, carrying out centrifugal separation on the materials to obtain a gypsum product I (the main components are shown in a table 4, and the particle size is shown in a table 5), carrying out deep calcium removal reaction on the waste liquid to obtain sodium chloride refined liquid, and returning to carry out salt separation to prepare sodium chloride.

Example two

Taking the second hazardous waste incineration wet deacidification wastewater as a raw material, pretreating the second hazardous waste incineration wet deacidification wastewater, then feeding the pretreated second hazardous waste incineration wet deacidification wastewater into a nanofiltration device to realize primary salt separation, and feeding the obtained high-purity sulfate waste liquid into an evaporation crystallization salt separation device to obtain a sodium sulfate product; the waste incineration fly ash II enters a fly ash washing device, soluble salts such as chloride and the like enter the solution, the solution is pretreated and then enters a nanofiltration device to realize primary salt separation, and the obtained sodium and potassium solution wastewater enters an evaporation crystallization salt separation device to obtain potassium chloride and sodium chloride products; and (4) the chlorine salt produced water obtained by nanofiltration and the calcium salt are produced and enter a gypsum synthesis device, and finally gypsum and sodium chloride are co-produced, so that comprehensive recycling is realized.

The method comprises the following specific steps:

pumping the hazardous waste incineration wet deacidification wastewater from a raw water storage tank to a pretreatment device, then pumping the hazardous waste incineration wet deacidification wastewater into a sulfate nanofiltration device through a high-pressure pump, separating sulfate and chloride and storing the sulfate and the chloride in a chloride generation storage tank and a sulfate storage tank respectively, obtaining a sodium sulfate crystallization product II (the main components are shown in table 1) after the sulfate waste liquid passes through an evaporation crystallization system, temporarily storing the evaporation mother liquid in the evaporation mother liquid storage tank, returning the evaporation mother liquid to the evaporation system, and returning the evaporation mother liquid to the nanofiltration device for treatment when the chloride is enriched to a certain concentration; the method comprises the following steps that fly ash passes through a fly ash washing device, the washed fly ash is transported to landfill or outsourcing recycling, washing waste liquid enters a nanofiltration salt separation device through a high-pressure pump after being pretreated, calcium salt, sodium salt and potassium salt are separated and then are respectively stored in a calcium salt water production storage tank and a sodium salt water production storage tank and a potassium salt water production storage tank, sodium salt waste liquid and potassium salt waste liquid respectively obtain a sodium chloride crystal product II (the main components are shown in a table 2) and a potassium chloride crystal product II (the main components are shown in a table 3) after passing through an evaporation crystallization salt separation device, evaporation mother liquid is temporarily stored in an evaporation mother liquid storage tank and returns to the evaporation crystallization salt separation device to continue salt separation and crystallization, and when calcium ions are enriched to a certain extent, the calcium ions are removed through the nanofiltration salt separation device; the method comprises the steps of respectively controlling the feeding flow rates of chlorine salt waste liquid and calcium salt waste liquid, respectively feeding the chlorine salt waste liquid and the calcium salt waste liquid into a gypsum synthesis kettle in a convection mode, controlling the feeding speeds of the chlorine salt waste liquid and the calcium salt waste liquid to be m (Ca) < m (SO4) > 1.1, controlling the residence time of a solution in the gypsum synthesis kettle and the gypsum crystallization kettle to be 6 hours, reacting residual sulfate radicals/sodium sulfate in chlorine salt with calcium salt to synthesize calcium sulfate gypsum and sodium chloride, automatically flowing synthetic slurry to the gypsum crystallization kettle through an overflow port, further completely reacting, ensuring longer residence time of synthetic particles, growing calcium sulfate crystals, being more beneficial to solid-liquid separation and improving the product quality, obtaining a gypsum product II (the main components are shown in a table 4 and the particle size is shown in a table 5) after materials are centrifugally separated, obtaining sodium chloride refined liquid after the waste liquid passes through a deep calcium removal reaction device, and returning to separate salt to prepare the sodium chloride.

Example three

Taking hazardous waste incineration wet deacidification wastewater III as a raw material, pretreating the hazardous waste incineration wet deacidification wastewater III, then feeding the hazardous waste incineration wet deacidification wastewater into a nanofiltration device to realize primary salt separation, and feeding the obtained high-purity sulfate waste liquid into an evaporation crystallization salt separation device to obtain a sodium sulfate product; the waste incineration fly ash III enters a fly ash washing device, soluble salts such as chloride and the like enter the solution, the solution is pretreated and then enters a nanofiltration device to realize primary salt separation, and the obtained sodium and potassium solution wastewater enters an evaporation crystallization salt separation device to obtain potassium chloride and sodium chloride products; and (4) the chlorine salt produced water obtained by nanofiltration and the calcium salt are produced and enter a gypsum synthesis device, and finally gypsum and sodium chloride are co-produced, so that comprehensive recycling is realized.

The method comprises the following specific steps:

pumping the hazardous waste incineration wet deacidification wastewater from a raw water storage tank to a pretreatment device, then pumping the hazardous waste incineration wet deacidification wastewater into a sulfate nanofiltration device through a high-pressure pump, separating sulfate and chloride and storing the sulfate and the chloride in a chloride generation storage tank and a sulfate storage tank respectively, obtaining a sodium sulfate crystal product III (the main components are shown in table 1) after the sulfate waste liquid passes through an evaporation crystallization system, temporarily storing the evaporation mother liquid in the evaporation mother liquid storage tank, returning the evaporation mother liquid to the evaporation system, and returning the evaporation mother liquid to the nanofiltration device for treatment when the chloride is enriched to a certain concentration; the method comprises the following steps that fly ash passes through a fly ash washing device, the washed fly ash is transported to landfill or outsourcing recycling, washing waste liquid enters a nanofiltration salt separation device through a high-pressure pump after being pretreated, calcium salt, sodium salt and potassium salt are separated and then are respectively stored in a calcium salt water production storage tank and a sodium salt water production storage tank and a potassium salt water production storage tank, sodium salt waste liquid and potassium salt waste liquid respectively obtain a sodium chloride crystal product III (the main components are shown in a table 2) and a potassium chloride crystal product III (the main components are shown in a table 3) after passing through an evaporation crystallization salt separation device, evaporation mother liquid is temporarily stored in an evaporation mother liquid storage tank and returns to the evaporation crystallization salt separation device to continue salt separation and crystallization, and when calcium ions are enriched to a certain extent, the calcium ions are removed through the nanofiltration salt separation device; respectively controlling the feeding flow of the chlorine salt waste liquid and the calcium salt waste liquid, respectively feeding the chlorine salt waste liquid and the calcium salt waste liquid into a gypsum synthesis kettle in a convection mode, controlling the feeding speed of the chlorine salt waste liquid and the calcium salt waste liquid to be m (Ca) < m (SO4) > 1.2, controlling the retention time of the solution in the gypsum synthesis kettle and the gypsum crystallization kettle to be 12 hours, reacting residual sulfate radical/sodium sulfate in the chlorine salt with the calcium salt to synthesize calcium sulfate gypsum and sodium chloride, automatically flowing the synthesized slurry to the gypsum crystallization kettle through an overflow port, further completely reacting, ensuring longer retention time of synthesized particles, growing calcium sulfate crystals, being more beneficial to solid-liquid separation and improving the product quality, obtaining a gypsum product III (the main components are shown in a table 4 and the particle size is shown in a table 5) after the materials are subjected to centrifugal separation, obtaining sodium chloride refined liquid after the waste liquid passes through a deep calcium removal reaction device, and returning to salt separation to prepare the sodium chloride.

TABLE 1 sodium sulfate product test results

TABLE 2 sodium chloride product test results

TABLE 3 detection results of potassium chloride products

TABLE 4 detection results of Gypsum Fibrosum products

TABLE 5 Gypsum product particle size test results

The method for the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash water washing provided by the embodiment of the invention at least has the following advantages:

1. the salt separation and crystallization process is simplified, and the product quality is improved; after nanofiltration treatment, the fly ash water washing wastewater is changed into a potassium-sodium binary system from high-salinity wastewater of a calcium, potassium-sodium ternary system, and deacidification wastewater is changed into high-purity sodium sulfate wastewater, evaporation salt separation crystallization is performed on the basis, so that the subsequent salt separation crystallization process flow is greatly simplified, the evaporation cost and the power consumption are reduced, and the quality of a crystallized product is improved;

2. the waste is treated by waste, and gypsum and sodium chloride are co-produced by synergistic treatment, so that comprehensive recycling is achieved; sulfate radicals in the chlorine salt production water and calcium chloride in calcium salt production water obtained by washing fly ash with water are used as raw materials to obtain calcium sulfate and refined sodium chloride, and the salt in the wastewater is fully recycled;

3. the production efficiency and the product quality are improved, large-particle calcium sulfate is directly obtained through the synthetic crystallization process, the product quality and the solid-liquid separation effect are improved, and the defects that a large amount of steam is consumed for evaporation salt separation crystallization, the process flow is long and the like are avoided; the gypsum synthesis system uses a synthesis and crystallization two-stage device, and meanwhile, guide cylinders are arranged in the synthesis kettle and the crystallization kettle and finally automatically flow to the gypsum crystallization kettle through an overflow port, so that the residence time of gypsum synthesis crystallization particles is greatly increased, and the growth of calcium sulfate crystals and thorough reaction are facilitated; the overflow port is arranged on the gypsum crystallization kettle, and under the stirring action, calcium sulfate with smaller crystallization particles returns to the gypsum synthesis kettle from the overflow port to continue the synthesis crystallization reaction and grow up, so that the large-particle high-quality calcium sulfate gypsum is obtained, and the problems that the particles of the gypsum mud obtained in the prior art are amorphous, the impurity content is large, the solid-liquid separation is difficult, the water content is high and the like are solved;

4. the production cost is reduced: the problems of high cost and large consumption when the incineration wet deacidification wastewater and the fly ash washing wastewater are independently subjected to harmless treatment are solved;

5. the method is environment-friendly and easy to popularize: the used process does not introduce a new pollution source, is environment-friendly, has strong operability, mature equipment manufacture and is easy for engineering popularization and application.

The system for the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash washing according to the embodiment of the invention is further described with reference to fig. 2, fig. 3 and fig. 4. The system for the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash washing can be used for realizing the method for the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash washing.

The system for the cooperative treatment of deacidification by the hazardous waste incineration method and fly ash washing comprises three parts: a hazardous waste incineration wet deacidification wastewater treatment unit, a fly ash washing wastewater treatment unit and a gypsum synthesis unit.

Wherein, referring to fig. 2, the hazardous waste incineration wet deacidification wastewater treatment unit mainly comprises: the hazardous waste incineration wet deacidification wastewater pretreatment device 2 is used for obtaining hazardous waste incineration wet deacidification wastewater and pretreating the hazardous waste incineration wet deacidification wastewater; the nanofiltration device 3 is connected with the hazardous waste incineration wet deacidification wastewater pretreatment device 2 and is used for carrying out nanofiltration treatment on the pretreated hazardous waste incineration wet deacidification wastewater to obtain sulfate waste liquid and chloride waste liquid; and the evaporative crystallization device 6 is connected with the nanofiltration device 3 and is used for carrying out evaporative crystallization treatment on the sulfate waste liquid to obtain sulfate crystals.

Exemplarily, the hazardous waste incineration wet deacidification wastewater treatment unit further comprises a raw water storage tank 1. After the hazardous waste incineration wet deacidification wastewater is pumped from the raw water storage tank 1 to the hazardous waste incineration wet deacidification wastewater pretreatment device 2, the hazardous waste incineration wet deacidification wastewater enters the nanofiltration device 3 through the high-pressure pump, so that the sulfate waste liquid and the chloride waste liquid are separated and respectively stored in the chloride water production storage tank 4 and the sulfate water production storage tank 5. The sulfate water production storage tank 5 is connected with the evaporative crystallization device 6, the sulfate waste liquid can obtain a sodium sulfate crystallization product after passing through the evaporative crystallization device 6, the evaporation mother liquid is temporarily stored in the first evaporation mother liquid storage tank 7 and returns to the evaporation system, and when the chlorine salt is enriched to a certain concentration, the chlorine salt returns to the nanofiltration device 3 for treatment. The chlorine salt water production storage tank 4 is connected with a gypsum synthesis unit.

Referring to fig. 3, the fly ash washing wastewater treatment unit mainly comprises: the fly ash washing device 8 is used for washing fly ash to obtain fly ash washing wastewater; the flying ash washing wastewater pretreatment device is connected with the flying ash washing device 8 and is used for pretreating the flying ash washing wastewater; the nanofiltration salt separation device 9 is connected with the flying ash washing wastewater pretreatment device and is used for carrying out nanofiltration salt separation treatment on the pretreated flying ash washing wastewater so as to separate calcium salt waste liquid and sodium potassium salt waste liquid; and the evaporative crystallization salt separation device 12 is connected with the nanofiltration salt separation device 9 and is used for carrying out evaporative crystallization salt separation treatment on the sodium potassium salt waste liquid to obtain sodium chloride crystals and potassium chloride crystals.

Illustratively, the fly ash is washed by a fly ash washing device 8, the washed fly ash is transported to landfill or outsourcing for recycling, the fly ash washing wastewater is pretreated by a fly ash washing wastewater pretreatment device and filtered by a bag filter, then enters a nano-filtration salt separation device 9 by a high-pressure pump, the nano-filtration salt separation device 9 separates calcium salt from sodium salt and potassium salt in the washing wastewater, and the obtained calcium salt wastewater and the sodium and potassium salt wastewater are respectively stored in a calcium salt water production storage tank 10 and a sodium and potassium salt water production storage tank 11. The sodium and potassium salt water production storage tank 11 is connected with an evaporative crystallization salt separation device 12, sodium and potassium salt waste liquid enters the evaporative crystallization salt separation device 12, sodium chloride and potassium chloride crystallization products are respectively obtained after evaporation crystallization salt separation, an evaporation mother liquid is temporarily stored in a second evaporation mother liquid storage tank 13, the evaporation mother liquid returns to an evaporation system to be subjected to salt separation crystallization continuously, and when calcium ions are enriched to a certain extent, the calcium ions are returned to a nanofiltration salt separation device 9 to be treated and removed. The calcium salt water-producing storage tank 10 is connected with a gypsum synthesis unit.

The gypsum synthesis unit includes a gypsum synthesis apparatus. Referring to fig. 4, the gypsum synthesis apparatus includes: a gypsum synthesis kettle 14 for obtaining the chlorine salt waste liquid and the calcium salt waste liquid, and reacting sulfate radicals in the chlorine salt waste liquid with calcium salts in the calcium salt waste liquid to generate calcium sulfate crystals; a gypsum crystallization kettle 15 for obtaining waste liquid in the gypsum synthesis kettle and growing the calcium sulfate crystals; and the centrifugal device is used for carrying out centrifugal separation on the waste liquid in the gypsum crystallization kettle to obtain gypsum.

Specifically, the charging flow rates of the chloride salt water and the calcium salt water are respectively controlled, the chloride salt water and the calcium salt water are respectively added into the gypsum synthesis kettle 14 in a convection manner, and the residual sulfate radical/sodium sulfate in the chloride salt reacts with the calcium salt to synthesize calcium sulfate gypsum and sodium chloride. All set up the draft tube in synthetic cauldron 14 of gypsum and the gypsum crystallization cauldron 15, synthetic cauldron 14 of gypsum has first overflow mouth, and synthetic thick liquid flows to gypsum crystallization cauldron 15 through first overflow mouth automatically, further thorough reaction here, guarantees longer dwell time simultaneously, and calcium sulfate crystal grows up, more does benefit to solid-liquid separation and improves product quality. The gypsum crystallization kettle 15 is provided with a second overflow port, and calcium sulfate with smaller crystallization particles returns to the gypsum synthesis kettle 14 from the second overflow port under the stirring action to continue the synthesis crystallization reaction and grow up. And (3) centrifugally separating the materials in the gypsum crystallization kettle 15 to obtain a gypsum product, allowing the waste liquid to pass through a deep calcium removal reaction device 16 to obtain a sodium chloride refined liquid, and returning the sodium chloride refined liquid to the fly ash washing wastewater treatment unit for nanofiltration salt separation treatment to obtain a sodium chloride product.

The further details of the system for the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash washing in the embodiment of the invention can be referred to above, and are not described herein any more, and the system performs the cooperative disposal of the hazardous waste incineration wet deacidification and the fly ash washing, so that the comprehensive recycling of the high-salt waste liquid is realized.

The present invention has been illustrated by the above embodiments, but it should be understood that the above embodiments are for illustrative and descriptive purposes only and are not intended to limit the invention to the scope of the described embodiments. Furthermore, it will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that many variations and modifications may be made in accordance with the teachings of the present invention, which variations and modifications are within the scope of the present invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.