WO2019181385A1 - 塩素含有粉体の脱塩処理方法及び塩素含有粉体の脱塩処理装置 - Google Patents
塩素含有粉体の脱塩処理方法及び塩素含有粉体の脱塩処理装置 Download PDFInfo
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- WO2019181385A1 WO2019181385A1 PCT/JP2019/007307 JP2019007307W WO2019181385A1 WO 2019181385 A1 WO2019181385 A1 WO 2019181385A1 JP 2019007307 W JP2019007307 W JP 2019007307W WO 2019181385 A1 WO2019181385 A1 WO 2019181385A1
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- desalting
- chlorine
- liquid
- washing liquid
- washing
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/38—Preparing or treating the raw materials individually or as batches, e.g. mixing with fuel
Definitions
- the present invention relates to a method for desalinating a chlorine-containing powder and a desalting treatment of a chlorine-containing powder, which are useful for desalinating a chlorine-containing powder such as incinerated ash and effectively using it as a cement raw material. Relates to the device.
- waste containing chlorine may cause problems such as blockage of cement production facilities due to the chlorine. Therefore, in order to use waste containing chlorine, such as incineration ash, as a raw material for cement, it is used after reducing the amount of chlorine contained in the incineration ash by desalting.
- Patent Document 1 discloses a method of dehydrating after adding water to incineration ash to elute chlorine.
- Patent Document 2 discloses a method of desalting by washing the incinerated ash a plurality of times by repeating mixing with water and dehydration.
- Patent Document 1 a large amount of water is required for desalting incineration ash. Therefore, in areas where a large amount of industrial water (fresh water) cannot be used, When the use of fresh water is restricted, it is difficult to use the method.
- Patent Document 3 discloses a method of using seawater in desalinating chlorine-containing powder such as incinerated fly ash for the purpose of cement raw material.
- JP 2002-338312 A Japanese Patent Laid-Open No. 2003-211129 JP 2013-166135 A
- Patent Document 3 is suitable for the purpose of not using a large amount of industrial water (fresh water), further examination is necessary to efficiently perform the desalting treatment of the chlorine-containing powder. .
- an object of the present invention is to provide a desalination treatment method and desalting that do not cause wasteful drainage by efficiently performing the desalination treatment of chlorine-containing powder using seawater or the like.
- the object is to provide a salt treatment apparatus.
- a step of washing the first desalted cake with a second desalting wash separate from the first desalting wash to obtain a second desalted cake and a second filtrate;
- the present invention provides a method for desalinating chlorine-containing powder, which is repeated for each chlorine-containing powder.
- the chlorine-containing powder is mixed with the first desalting washing liquid to form a slurry, and the chlorine contained in the chlorine-containing powder is eluted into the liquid phase of the slurry.
- a part or all of the liquid phase is separated from the slurry to obtain a first desalted cake, and the first desalted cake is further separated from the first desalted washing liquid.
- cleaning process circulate and use at least one part as 1st desalting washing liquid, By repeating the above treatment for each supplied chlorine-containing powder, the amount of washing water used as the first desalting washing liquid can be reduced per one chlorine-containing powder.
- the first desalting washing liquid has no significant influence on the chlorine removal efficiency from the chlorine-containing powder up to a predetermined upper limit concentration even when the chlorine ion concentration exceeds the chlorine ion concentration of seawater, for example. It is possible to achieve both the merit of reducing the use amount of chlorine and the efficiency of chlorine removal. Furthermore, since the treatment is performed while controlling the chlorine ion concentration of the first desalting washing solution, when the chlorine ion concentration of the first desalting washing solution becomes unsuitable for treatment, the treatment should be corrected at an appropriate timing. Is possible.
- the present invention secondly, in the method for desalinating a chlorine-containing powder, when the chlorine ion concentration of the first desalting washing liquid exceeds a first threshold, the present invention provides a desalting treatment method in which a washing solution for 1 desalting is controlled so as to satisfy the first threshold value with a new first desalting washing solution.
- the chlorine ion concentration of the first desalting washing liquid increases. If it becomes a tendency and eventually exceeds a predetermined upper limit concentration, the chlorine removal efficiency may be affected in some cases, but a decrease in the chlorine removal efficiency can be prevented beforehand.
- the first threshold value a desired value may be set as appropriate based on, for example, evaluation of a trial run. More typically, for example, the chlorine ion concentration of the first desalting washing liquid constituting the slurry with the chlorine-containing powder is 15% by mass.
- the chlorine removal efficiency may be affected.
- the present invention thirdly uses seawater as the first first desalting washing liquid added to the chlorine-containing powder in the chlorine-containing powder desalting method,
- the present invention provides a desalting method in which the chlorine ion concentration of the first desalting washing solution does not exceed 15% by mass.
- the chlorine ion concentration of seawater is approximately 3% by mass, even when the first desalting washing liquid is mainly composed of seawater, the chlorine ion concentration is approximately 3% by mass to It is easy to keep in the range of about 15% by mass, and multiple treatments of at least two times or more are possible for each chlorine-containing powder to be supplied. Therefore, the merit of reduction of the usage-amount of engineering water (fresh water) etc. is acquired. Further, when seawater is used as the first desalting washing solution, it is considered to be an effect of seawater as a buffer solution, but heavy metals from incineration fly ash and the like (specifically, Pb, Zn, etc.). The effect of suppressing elution of is observed.
- drain containing heavy metals is reduced. Furthermore, when the chlorine ion concentration of the first desalting washing liquid exceeds 15% by mass, the chlorine removal efficiency may be affected depending on the case, but the reduction of the chlorine removal efficiency can be prevented beforehand. .
- the second filtrate obtained in the desalting cake washing step is at least partly in the second desalting process. 2 circulated and used as a desalting wash, while controlling the chlorine ion concentration of the second desalting wash, the slurrying step, the chlorine elution step, the desalting cake forming step,
- the present invention provides a desalting treatment method in which a desalting cake washing step is repeated for each supplied chlorine-containing powder.
- cleaning process circulates and uses at least one part as a 2nd desalting washing
- the amount of washing water used as the second desalting washing liquid per one chlorine-containing powder can be reduced.
- the chlorine ion concentration of the second desalting washing liquid tends to increase, and thus remains in the second desalting cake.
- Chlorine ion concentration tends to increase. For example, if it is used as it is, it tends to be difficult to use it as a cement raw material.
- the treatment is performed while controlling the chlorine ion concentration of the second desalting washing liquid, the second desalting is performed. When the chlorine ion concentration of the washing liquid becomes unsuitable for treatment, it can be corrected at an appropriate timing.
- the chlorine ion concentration of the second desalting washing liquid is different from the first threshold value.
- the desalting treatment method of controlling the second desalting washing solution to satisfy the second threshold value with a new second desalting washing solution is provided. It is.
- the chlorine ion concentration of the second desalting washing solution tends to increase.
- the chloride ion concentration remaining in the salt cake tends to increase.
- a desired value may be set as appropriate based on, for example, evaluation of a trial run. More typically, for example, the chlorine ion concentration of the second desalting washing liquid for washing the first desalting cake is 3.5% by mass.
- the chlorine ion concentration remaining in the obtained second desalted cake can be used as a raw material for cement as it is, for example.
- a washing liquid having a lower chlorine ion concentration for example, industrial water, may be used as a cement raw material. Additional cleaning with (fresh water) is required.
- the second desalting washing liquid has a chlorine ion concentration of 3.5 mass. %, The desalting method is provided.
- the 2nd desalting washing liquid for wash cleaning a 1st desalting cake
- the chlorine ion concentration is made not to exceed 3.5 mass%
- the 2nd desalting obtained is carried out. Since the chlorine ion concentration of the liquid phase remaining in the salt cake does not exceed the concentration, it can be used as a raw material for cement as it is, for example.
- the present invention seventhly provides a desalting treatment method for a chlorine-containing powder, further comprising the following steps (1) to (3): It is.
- the waste liquid obtained by desalting incineration fly ash and the like normally contains heavy metals, but after collecting the waste liquid, adding a heavy metal scavenger to agglomerate By insolubilizing in a floc form and removing it as a heavy metal agglomerated cake, it is possible to prevent drainage liquid containing heavy metals from being discharged out of the system.
- the obtained heavy metal agglomerated cake can be effectively used as a cement raw material.
- the present invention provides, in the eighth aspect, in the seventh desalinating method of chlorine-containing powder, further comprising the following step (4): is there. (4) The first agglomerated cake is washed with a third desalting washing liquid different from the first desalting washing liquid and the second desalting washing liquid to obtain a second agglomerated cake and a fourth filter. Heavy metal agglomerated cake washing process to obtain liquid
- the 2nd aggregation cake from which chlorine was fully removed can be obtained by wash
- the heavy metal insolubilization step sets the pH of the drainage to 7 to 11.
- the present invention provides a desalting method.
- the fourth filtrate obtained in the heavy metal agglomerated cake washing step is at least a part thereof. Is used as the first desalting washing solution to provide the desalting treatment method.
- cleaning utilized as a 1st desalting washing liquid.
- the amount of water used can be reduced.
- the second filtrate obtained in the desalting cake washing step is at least a part thereof.
- the third desalting washing liquid and / or the fourth filtrate obtained in the heavy metal agglomerated cake washing step circulates and uses at least a part thereof as the third desalting washing liquid.
- the present invention provides a desalting treatment method in which the washing treatment in the heavy metal agglomerated cake washing step is performed while controlling the chlorine ion concentration of the third desalting washing solution.
- cleaning process utilizes the at least one part as a 3rd desalting washing
- the chlorine ion concentration of the third desalting washing liquid is the first threshold value and the first desalting method.
- the third threshold value which is different from the second threshold value, is exceeded, the third desalting washing liquid is controlled by the new third desalting washing liquid so as to satisfy the third threshold value.
- the second filtrate is used as part or all of the third desalting washing liquid and / or the fourth filtrate is circulated as part or all of the third desalting washing liquid.
- the chlorine ion concentration of the third desalting washing liquid tends to increase, and consequently the chlorine ion concentration remaining in the second agglomerated cake tends to increase.
- the chloride ion concentration may be set as appropriate based on, for example, evaluation of a trial run.
- the chlorine ion concentration of the third desalting washing liquid for washing the first agglomerated cake is 3.5% by mass. If the chlorine ion concentration is 3.5% by mass or less, the chlorine ion concentration remaining in the obtained second agglomerated cake can be used as a raw material for cement as it is, for example. On the other hand, if the chlorine ion concentration of the third desalting washing liquid exceeds 3.5% by mass, the washing liquid having a lower chlorine ion concentration, for example, industrial water, may be used as a cement raw material in some cases. Additional cleaning with (fresh water) is required.
- the chlorine ion concentration of the third desalting washing liquid exceeds 3.5 mass%.
- the present invention provides the desalting method.
- the 2nd aggregation cake obtained Since the concentration of chlorine ions in the liquid phase remaining therein does not exceed the vicinity of the concentration, for example, it can be used as it is as a cement raw material.
- the chlorine-containing powder is selected from incineration fly ash, molten fly ash, and chlorine bypass dust.
- the present invention provides the desalting treatment method including one or more kinds.
- cement raw materials such as incineration fly ash, molten fly ash, and chlorine bypass dust, which are wastes containing chlorine.
- a first desalting washing liquid supply device for supplying a first desalting washing liquid;
- the chlorine-containing powder is mixed with the first desalting washing liquid from the first desalting washing liquid supply device to form a slurry, and the chlorine contained in the chlorine-containing powder in the slurry is in a liquid phase.
- An elution tank for eluting in A first solid-liquid separator that performs a process of separating a part or all of the liquid phase from the slurry from which chlorine has been eluted to obtain a first desalted cake and a first filtrate; A slurry conveying device for conveying the slurry treated in the elution tank to the first solid-liquid separation device; In the first solid-liquid separator, the first desalted cake and the second filtrate are washed by washing the first desalted cake with a second desalting wash separate from the first desalting wash.
- a second desalting washing liquid supply device for supplying the second desalting washing liquid so as to perform a process to obtain;
- a first liquid feeding device for feeding the second filtrate obtained in step 1 to the first desalting washing liquid supply device in order to circulate and use at least part of the second filtrate as the first desalting washing liquid.
- the present invention provides a chlorine-containing powder desalting apparatus comprising a first chlorine ion concentration monitoring device for monitoring the chlorine ion concentration of the first desalting washing solution.
- the above-described chlorine-containing powder desalting method can be effectively carried out.
- the first liquid feeding device since the first liquid feeding device is provided, the first filtrate obtained by the first desalting cake forming process performed by the first solid-liquid separation device and / or the first solid-liquid separation device is used. Since at least a part of the second filtrate obtained by the washing treatment of the first desalting cake is circulated and used as the first desalting washing solution, and the treatment is repeated for each chlorine-containing powder to be supplied. The amount of washing water used as the first desalting washing solution per chlorine-containing powder can be reduced.
- the chlorine ion concentration of the first desalting washing liquid tends to increase, If the chlorine ion concentration of the desalting washing liquid exceeds a predetermined upper limit concentration, the chlorine removal efficiency may be affected in some cases. However, the chlorine ion concentration in the first desalting washing liquid may be monitored. By providing the 1 chlorine ion concentration monitoring device, when the chlorine ion concentration of the first desalting washing liquid becomes unsuitable for processing, it can be corrected at an appropriate timing.
- the chlorine-containing powder desalination apparatus further includes a new desalting solution for supplying a new first desalting washing solution as the first desalting washing solution to the first desalting washing supply device.
- a first desalting washing liquid supply device; The first desalting washing liquid supply device is configured to change a supply amount of the first desalting washing liquid from the first desalting washing liquid supply device to the elution tank.
- the new first desalting washing liquid supply apparatus includes a second supply regulating valve that makes the supply amount of the washing liquid to the first desalting washing liquid supply apparatus variable.
- the first desalting washing supply apparatus controls the first desalting washing control device by controlling the first supply regulating valve.
- the desalinization apparatus configured to supply the new first desalting washing solution is provided.
- a new supply device for the first desalting washing liquid is provided, and when the first threshold value is exceeded under the monitoring by the first chlorine ion concentration monitoring device, the first threshold value is set so as to satisfy the first threshold value. Since a new first desalting washing solution is supplied to the 1 desalting washing supply device, if the chlorine ion concentration of the first desalting washing solution exceeds a predetermined upper limit concentration, chlorine Although the removal efficiency may be affected, a decrease in the chlorine removal efficiency can be prevented in advance.
- a desired value may be set as appropriate based on, for example, evaluation of a trial run.
- the chlorine ion concentration of the first desalting washing liquid constituting the slurry with the chlorine-containing powder is 15% by mass. If the chlorine ion concentration does not exceed 15% by mass, the elution efficiency of chlorine from the chlorine-containing powder into the liquid phase of the slurry is not so much affected, that is, the chlorine removal efficiency is not so much affected. On the other hand, when the chlorine ion concentration of the first desalting washing liquid exceeds 15% by mass, the chlorine removal efficiency may be affected.
- the chlorine-containing powder demineralization apparatus further comprises: In order to circulate and use at least a part of the second filtrate obtained by the washing treatment of the first desalted cake performed in the first solid-liquid separator as the second desalting washing solution, A second liquid feeding device for feeding the washing liquid supply device for 2 desalting;
- the present invention provides a desalting apparatus comprising a second chlorine ion concentration monitoring device for monitoring the chlorine ion concentration of the second desalting washing solution.
- the second liquid feeding device by providing the second liquid feeding device, at least a part of the second filtrate obtained by the washing treatment of the first desalted cake made by the first solid-liquid separator is washed for the second desalting. Since the treatment is repeated for each chlorine-containing powder that is circulated and used as a liquid, the amount of washing water used as the second desalting washing liquid can be reduced per one chlorine-containing powder. . Further, when the second filtrate is circulated and used as part or all of the second desalting washing solution, the chlorine ion concentration of the second desalting washing solution tends to increase, and as a result remains in the second desalting cake.
- the chlorine ion concentration tends to increase, and for example, if it is used as it is, it tends to be difficult to use it as a cement raw material, but it is equipped with a second chlorine ion concentration monitoring device for monitoring the chlorine ion concentration of the second desalting washing solution.
- a second chlorine ion concentration monitoring device for monitoring the chlorine ion concentration of the second desalting washing solution.
- the chlorine-containing powder desalting apparatus further includes a new desalting solution for supplying a new second desalting washing solution as the second desalting washing solution to the second desalting washing supply device.
- a second desalting solution supply device makes the supply amount of the second desalting washing liquid from the second desalting washing liquid supply device to the first desalting cake variable, Comprising a third supply regulating valve that allows draining from the second desalting washing liquid supply device;
- the new second desalting washing liquid supply apparatus includes a fourth supply regulating valve that makes the supply amount of the washing liquid variable to the second desalting washing liquid supply apparatus, When the chlorine ion concentration of the second desalting washing liquid exceeds a second threshold value different from the first threshold value, the second desalting washing liquid supply is controlled by controlling the third supply regulating valve.
- the second desalting washing liquid supply device is controlled by controlling the fourth supply regulating valve of the new second desalting washing liquid supply device.
- the demineralization treatment apparatus is configured to supply the new second desalting washing liquid so as to satisfy the second threshold as the washing liquid.
- a new second desalting washing liquid supply device is provided, and when the second threshold value is exceeded under the monitoring by the second chlorine ion concentration monitoring device, the second threshold value is satisfied so as to satisfy the second threshold value. 2 Since a new second desalting washing solution is supplied to the desalting washing supply device, if the chlorine ion concentration of the second desalting washing solution exceeds a predetermined upper limit concentration, Although it becomes difficult to make the obtained desalted cake as a raw material for cement as it is, it is possible to prevent the chlorine ion concentration from exceeding a predetermined upper limit concentration.
- the second threshold value a desired value may be set as appropriate based on, for example, evaluation of a trial run. More typically, for example, the chlorine ion concentration of the second desalting washing liquid for washing the first desalting cake is 3.5% by mass. If the chlorine ion concentration is 3.5% by mass or less, the chlorine ion concentration remaining in the obtained second desalted cake can be used as a raw material for cement as it is, for example. On the other hand, when the chlorine ion concentration of the second desalting washing liquid exceeds 3.5% by mass, in some cases, a washing liquid having a lower chlorine ion concentration, for example, industrial water, may be used as a cement raw material. Additional cleaning with (fresh water) is required.
- the chlorine-containing powder demineralization treatment apparatus further comprises: Of the first filtrate and the second filtrate, those not reused as the first desalting washing liquid or the second desalting washing liquid, drained from the first desalting washing liquid supply device One selected from the group consisting of the first desalting washing liquid sent as a liquid and the second desalting washing liquid sent as a drain from the second desalting washing supply apparatus Or, two or more kinds are collected and stored as drainage, and a heavy metal insolubilization reaction tank for insolubilizing heavy metals contained in the drainage into aggregated floc form by adding a heavy metal scavenger thereto, A second solid-liquid separator that performs a process of separating a part or all of the liquid phase from the agglomerated floc-containing liquid containing the insolubilized heavy metal to obtain a first agglomerated cake and
- the waste liquid from which desalted incineration fly ash, etc. normally contains heavy metals, but after collecting the waste liquid, a heavy metal collector is used. It can be added and insolubilized in the form of aggregated floc. And by providing the 2nd solid-liquid separation apparatus, it can prevent that the waste liquid containing heavy metals is discharged
- the chlorine-containing powder demineralization apparatus further comprises: In the second solid-liquid separation device, the second agglomerated cake and the fourth filtrate are washed with a third desalting washing liquid different from the first desalting washing liquid and the second desalting washing liquid.
- the demineralization treatment apparatus is provided, which includes a third demineralization washing liquid supply device for supplying the third demineralization washing liquid so as to perform the process of obtaining the above.
- a third desalting washing liquid supply device for supplying a third desalting washing liquid is provided, and the first agglomerated cake obtained in the heavy metal agglomerated cake forming step is washed by the third desalting washing liquid.
- the 2nd aggregation cake from which chlorine was fully removed can be obtained. Therefore, the obtained heavy metal agglomerated cake can be more suitably used as a cement raw material.
- the chlorine-containing powder demineralization apparatus further comprises: In order to circulate and use at least a part of the fourth filtrate obtained by the washing treatment of the first agglomerated cake made in the second solid-liquid separator as the first desalting washing solution,
- the present invention provides a desalting apparatus comprising a third liquid feeding device for feeding a washing liquid supply device for desalting.
- the chlorine-containing powder demineralization apparatus further comprises: In order to use at least a part of the second filtrate obtained by the washing treatment of the first desalted cake performed by the first solid-liquid separator as the third desalting washing solution, And / or a fourth liquid feeding device for feeding the washing liquid supply device for desalting, and / or In order to circulate and use at least a part of the fourth filtrate obtained by the washing treatment of the first agglomerated cake made in the second solid-liquid separator as the third desalting washing liquid, A fifth liquid feeding device for feeding the desalted washing liquid supply device;
- the present invention provides a desalting apparatus comprising a third chlorine ion concentration monitoring device for monitoring the chlorine ion concentration of the third desalting washing solution.
- the second filtrate obtained in the desalting cake washing step uses at least a part thereof as the third desalting washing liquid and / or the fifth liquid feeding.
- the fourth filtrate obtained in the heavy metal agglomerated cake washing step circulates and uses at least part of the fourth filtrate as the third desalting washing solution. The amount of water used can be reduced.
- the chlorine-containing powder demineralization apparatus further comprises the third desalting apparatus.
- a new third desalting cleaning liquid supply device for supplying a new third desalting cleaning liquid as the third desalting cleaning liquid to the cleaning liquid supply device;
- the third desalting washing liquid supply device makes the supply amount of the third desalting washing liquid from the third desalting washing liquid supply device to the first agglomerated cake variable.
- the new third desalting washing liquid supply apparatus includes a sixth supply regulating valve that makes the supply amount of the washing liquid variable to the third desalting washing liquid supply apparatus,
- the third desalting liquid is controlled by controlling the fifth supply regulating valve. Stop or reduce the supply of the third desalting washing liquid from the salt washing liquid supply device to the first agglomerated cake, and the third desalting washing liquid from the third desalting washing liquid supply device.
- the third desalting cleaning liquid supply device is controlled by controlling the sixth supply regulating valve of the new third desalting cleaning liquid supply device after draining part or all of
- the present invention provides the desalting apparatus configured to supply the new third desalting washing liquid so as to satisfy the third threshold as the third desalting washing liquid.
- a new third desalting washing liquid supply device is provided, and when the third threshold value is exceeded under monitoring by the third chlorine ion concentration monitoring device, the third threshold value is satisfied so that the third threshold value is satisfied. Since a new third desalting cleaning solution is supplied to the 3 desalting cleaning solution supply device, if the chlorine ion concentration of the third desalting cleaning solution exceeds a predetermined upper limit concentration, The resulting heavy metal agglomerated cake is difficult to be used as a cement raw material as it is, but it is possible to prevent the chloride ion concentration from exceeding a predetermined upper limit concentration.
- the third threshold value a desired value may be set as appropriate based on, for example, evaluation of a trial run. More typically, for example, the chlorine ion concentration of the third desalting washing liquid for washing the first agglomerated cake is 3.5% by mass. If the chlorine ion concentration is 3.5% by mass or less, the chlorine ion concentration remaining in the obtained second agglomerated cake can be used as a raw material for cement as it is, for example. On the other hand, if the chlorine ion concentration of the third desalting washing liquid exceeds 3.5% by mass, in some cases, the washing liquid having a lower chlorine ion concentration, for example, industrial water, may be used as a cement raw material. Additional cleaning with (fresh water) is required.
- the first solid-liquid separation device and the second solid-liquid separation device are the same.
- the present invention provides a desalting apparatus that performs the respective processes in the apparatus.
- the device configuration can be simplified by sharing the solid-liquid separation device to be used.
- FIG. 2 is an overall configuration flow diagram further illustrating the chlorine-containing powder desalting method and the chlorine-containing powder desalting apparatus according to the present invention.
- the first solid-liquid separation apparatus and the second solid-liquid separation apparatus are the same as each other.
- the case where the first solid-liquid separation device and the second solid-liquid separation device are the same device is further illustrative.
- the desalting object of the present invention is not particularly limited as long as it contains chlorine, and examples thereof include incineration fly ash, molten fly ash, and chlorine bypass dust. These are wastes that have been used effectively as a raw material for cement after desalination treatment, and the typical municipal waste incineration fly ash, that is, fly ash generated when incinerating household waste waste (this book) In the specification, it is simply referred to as “incineration fly ash”.)
- chlorine (Cl) is contained at a concentration of about 10% by mass to 30% by mass, and is generated from a gasification melting furnace.
- the fly ash (hereinafter simply referred to as “molten fly ash”) contains chlorine at a concentration of about 10% by mass to 40% by mass.
- chlorine bypass dust which is dust contained in cement kiln extraction gas, generally contains chlorine at a concentration of about 10% by mass to 40% by mass.
- the chlorine concentration of the chlorine-containing powder as described above is reduced to about 3% by mass or less, more typically to about 2% by mass or less, and this is effectively used as, for example, a cement raw material. Can do.
- the concentration of chlorine in the chlorine-containing powder can be measured by a well-known method.
- ISO 29581-2 Cement-Test methods-Part2 Chemical analysis by X-ray fluorescence, or Cement Association standard test method JCAS I- Preferred examples include X-ray fluorescence analysis and the like using 05 “Method for quantifying chlorine in cement by fluorescent X-ray analysis”.
- FIG. 1 is a flow chart showing a first embodiment of a method for desalinating chlorine-containing powder according to the present invention.
- the desalination treatment according to the present invention includes a slurrying step in which a chlorine-containing powder is mixed with a first desalting washing solution to form a slurry, and the chlorine-containing powder in the slurry. Elution step of eluting chlorine contained in the liquid phase into the liquid phase, and a desalting cake in which part or all of the liquid phase is separated from the slurry from which chlorine is eluted to obtain a first desalted cake and a first filtrate The forming step and the obtained first desalted cake are washed with a second desalting wash separate from the first desalting wash to obtain a second desalted cake and a second filtrate. A salt cake washing step.
- the first filtrate obtained in the desalting cake forming step and / or the second filtrate obtained in the desalting cake washing step is circulated and used at least in part as the first desalting washing solution,
- the above slurrying process, chlorine elution process, desalted cake forming process, and cake washing process are repeated for each chlorine-containing powder to be supplied. Thereby, since at least a part of the first desalting washing liquid and / or the second desalting washing liquid used once is recycled, it contributes to saving of washing water.
- monitoring means, for example, constantly monitoring the chlorine ion concentration of the first desalting washing solution, or sequentially sampling at a predetermined time, or arbitrarily sampling the concentration. It also includes the measurement of the above.
- Control means, for example, feedback control of the chlorine ion concentration of the first desalting washing solution so as not to exceed a predetermined threshold value, or a new first deionization at a predetermined timing or amount.
- the “first washing solution for desalting”, which is the object of “monitoring” or “control”, is simply to directly monitor or control the state of the washing solution forming a slurry with the chlorine-containing powder. If the target is the chlorine ion concentration of the first desalting wash before being added to the supplied chlorine-containing powder, or it is mixed with a new wash at a prescribed blending ratio and recycled. May target the chloride ion concentration of the pre-formulation. That is, the chlorine ion concentration of the first desalting washing liquid constituting the slurry with the supplied chlorine-containing powder may be substantially monitored and controlled.
- the chlorine ion concentration of the first desalting washing solution that goes around the system is excessively increased and the chlorine removal efficiency from the chlorine-containing powder from being lowered.
- the chlorine ion concentration of the first desalting washing liquid constituting the slurry exceeds a predetermined threshold
- the chlorine ion concentration of the first desalting washing liquid circulating in the system is arbitrarily adjusted.
- the first desalting washing solution may be renewed, and the treatment may be performed for each supplied chlorine-containing powder.
- the desalination object is incinerated fly ash, molten fly ash, or chlorine bypass dust.
- seawater itself (seawater accounts for 100%) is used as the first first desalting washing liquid of the repeated treatment, and the second desalting washing liquid is used as the first desalting washing liquid.
- the first one is repeatedly used without recirculation, about 2 to 4 times, more typically about 2 to 3 times, without newly adjusting the first desalting washing solution, It is possible to repeat the treatment of the supplied chlorine-containing powder.
- FIG. 2 is a flow chart showing a second embodiment of the method for desalinating chlorine-containing powder according to the present invention.
- the chlorine ion concentration of the second desalting washing solution that is repeatedly used increases with the number of repetitions, this is monitored and controlled.
- “monitoring” and “control” have the same meaning as in the case of the first desalting washing solution.
- the “second desalting washing liquid” that is the object of “monitoring” or “control” is not only directly monitoring or controlling the state of washing the first desalted cake, but also a predetermined composition. In the case of recirculating use after mixing with a new washing solution or the like at a ratio, the chlorine ion concentration of the pre-preparation may be targeted. That is, the chlorine ion concentration of the second desalting washing liquid constituting the washing liquid for washing the first desalting cake may be substantially monitored and controlled.
- the chlorine ion concentration of the second desalting washing solution circulating in the system is excessively increased, and chlorine ions remain at a high concentration in the second desalting cake obtained after washing the first desalting cake. Consequently, it can be prevented that it is difficult to use it as a cement raw material as it is.
- the chlorine ion concentration of the second desalting washing liquid for washing the first desalting cake exceeds a predetermined threshold
- the chlorine ion concentration of the second desalting washing liquid circulating in the system May be arbitrarily adjusted, or the second desalting washing solution may be renewed, and the treatment may be carried out for each chlorine-containing powder to be supplied.
- the second desalting washing liquid As a guideline for the number of times the second desalting washing liquid circulates around the system, it depends on the target to be desalted, but the desalted target is incinerated fly ash, molten fly ash, or chlorine bypass dust.
- the second desalting washing solution When industrial water (fresh water) is used as the second desalting washing solution, the second desalting washing solution is newly added about 2 to 4 times, more typically about 2 to 3 times. It is possible to repeat the treatment of the supplied chlorine-containing powder without adjustment.
- water other than seawater such as industrial water (fresh water), or a chloride ion concentration adjusting agent such as NaCl or KCl is optionally added thereto.
- Chlorine-containing water with adjusted chloride ion concentration may be used, but in areas where a large amount of industrial water (fresh water) cannot be used, or when the use of industrial water (fresh water) is restricted due to cost, etc. In, it is convenient to use seawater.
- seawater 100% by mass of the first desalting washing liquid may be occupied by seawater, or a mixed liquid of seawater and water other than seawater may be used.
- seawater occupies at least 50 mass% or more, and more preferably 75 mass% or more as seawater accounts for the first desalting wash.
- Pb which is the heavy metals, Zn or the like is less likely to elute into the liquid phase of the slurry composed of the first desalting washing solution, which contributes to a reduction in the treatment cost of waste water containing heavy metals. That is, for example, it is possible to reduce the amount of use of a redox potential adjusting agent, an inorganic flocculant, a polymer flocculant and the like necessary for the insolubilization treatment of heavy metals described later.
- the chlorine ion concentration of the first desalting washing solution added at the first iteration is preferably 2% by mass to 5% by mass, more preferably 2% by mass to 4% by mass. Most preferably, the content is from 3% by mass to 3% by mass.
- seawater itself seawater accounts for 100% by mass
- the chlorine ion concentration is about 3% by mass.
- the chlorine ion concentration of the first desalting washing solution added at the first iteration is less than the above range, it becomes difficult to use seawater as the first desalting washing solution as it is. Further, if the chlorine ion concentration of the first desalting washing solution added at the first time of the repeated treatment exceeds the above range, the number of repeated treatments cannot be gained, and there is not much contribution to saving the amount of washing water used. .
- the chlorine ion concentration of the first desalting washing liquid constituting the slurry with the chlorine-containing powder is preferably 3% by mass to 15% by mass, and 3% by mass to 10% by mass. Is more preferable, and 3% by mass to 5% by mass is particularly preferable. If this range is exceeded, the elution efficiency of chlorine into the liquid phase of the slurry composed of the first desalting washing solution is poor, and as a result, the chlorine removal efficiency may be impaired.
- the second desalting washing liquid used in the present invention is the same as the first desalting washing liquid in that seawater may be used.
- the chlorine ion concentration of the second desalting washing liquid for washing the desalted cake at the first iteration is 3.5% by mass or less. It is preferably 3% by mass or less, and most preferably 2.5% by mass or less.
- FIG. 3 is an overall configuration diagram showing the first embodiment of the chlorine-containing powder desalting apparatus according to the present invention.
- the desalination apparatus 1 includes a chlorine-containing powder P1 supplied from a chlorine-containing powder supply device 21 and a first desalting solution supplied from a first desalting washing liquid supply device 22.
- An elution tank 2 for storing the washing liquid W1 is provided.
- the chlorine-containing powder P1 is mixed with the first desalting washing liquid W1 to form a slurry, and the slurry is mixed and stirred for a predetermined time, whereby the chlorine contained in the chlorine-containing powder P1 is mixed. It is dissolved in the liquid phase and eluted.
- the elution tank 2 is provided with a stirring device 24, and the slurry can be mixed and stirred for a predetermined time by rotating the stirring blade 24a.
- the 1st solid-liquid separation apparatus 3 which solid-liquid-separates the slurry S1 discharged
- the first solid-liquid separator 3 a part or all of the liquid phase is separated from the slurry S1 to obtain the first desalted cake C1 and the first filtrate W3.
- a filter press is used as the first solid-liquid separator 3.
- the obtained first desalted cake C1 can be washed with the second desalting washing liquid W2 supplied from the second desalting washing liquid supply apparatus 31.
- a valve mechanism Va is provided in the middle of the path for transporting the slurry S1 processed in the elution tank 2 to the first solid-liquid separation device 3, while the second desalting washing liquid supply device 31
- Another valve mechanism Vb is also provided in the middle of the path through which the second desalting washing liquid W2 is circulated to the first solid-liquid separator 3, so that the slurry S1 and the second desalting washing liquid W2 are selectively used.
- the slurry S1 can be directed to the first solid-liquid separator 3 and processed by the first solid-liquid separator 3 to obtain the first desalted cake C1.
- the second desalting washing liquid W2 is directed to the first solid-liquid separator 3, and the first desalting cake C1 is washed thereby to obtain the second desalting cake C2 and the second filtrate W4.
- the first filtrate W3 generated by the desalting cake forming step and the second filtrate W4 generated by the desalting cake washing step are a predetermined valve mechanism.
- the first liquid delivery device 5 comprising a predetermined liquid delivery pump mechanism sends the liquid to the storage section of the first desalting washing liquid supply device 22 and circulates it as the first desalting washing liquid W1. Can be done. If desired, for example, when the chlorine ion concentration of the first filtrate W3 becomes too high, a part or all of the first filtrate W3 is directed outside the system via a predetermined valve mechanism Vd. It may be directed to the discharged liquid W5.
- the first chlorine ion concentration monitoring device 7 is provided in the storage portion of the first desalting washing liquid supply device 22, and the first desalting stored in the storage portion of the first desalting washing liquid supply device 22 is provided.
- the chloride ion concentration of the salt washing liquid W1 is monitored.
- a chlorine ion meter is used as the first chlorine ion concentration monitoring device 7.
- a general-purpose analysis method such as ion chromatography may be used for diluted water having an appropriate magnification.
- the 1st chlorine ion concentration monitoring apparatus 7 it arrange
- it may be arranged to be measurable at a position immediately before entering the storage part of the first desalting washing liquid supply device 22. That is, in any arrangement, it is sufficient that the chlorine ion concentration in the first desalting washing liquid W1 can be estimated.
- the first desalting washing liquid supply device 22 is provided with a first supply regulating valve 22a having a predetermined regulating valve mechanism, and the contents in the storage tank provided in the first desalting washing liquid supply device 22 are stored in the first tank. 1 It is possible to distribute by the first supply regulating valve 22a whether the desalting washing liquid W1 is directed to the elution tank 2 or discharged to the outside of the system by the first supply regulating valve 22a. To be able to adjust.
- the desalting apparatus 1 includes a new first desalting washing liquid for supplying a new first desalting washing liquid W1a to the first desalting washing liquid supply apparatus 22. Is added as a part of the first desalting washing liquid in the system, if desired, via a second supply regulating valve 23a comprising a predetermined regulating valve mechanism. Part or all of the first desalting washing liquid that has been used repeatedly can be replaced. In this case, the contents of the storage part of the first desalting washing liquid supply device 22 appropriately drain the amount corresponding to the amount supplied with the new first desalting washing liquid W1a toward the outside of the system. It may be directed to the liquid W5.
- the second desalting washing liquid supply device 31 is provided with a third supply regulating valve 31a having a predetermined regulating valve mechanism, and the contents in the storage tank provided in the second desalting washing liquid supply device 31 are stored in the second tank. 2 It is possible to sort by the third supply regulating valve 31a whether the desalting washing liquid W2 is directed to the first solid-liquid separation device 3 or the waste liquid W5 directed to the outside of the system. The amount of liquid to be directed to can be adjusted.
- the desalting apparatus 1 includes a new second desalting washing liquid for supplying a new second desalting washing liquid W2a to the second desalting washing supply apparatus 31. Is supplied as a part of the second desalting washing liquid in the system, if desired, via a fourth supply regulating valve 32a comprising a predetermined regulating valve mechanism. A part or all of the second washing solution for desalting used repeatedly can be replaced. In this case, the contents of the storage part of the second desalting washing liquid supply device 31 are appropriately discharged according to the amount supplied with the new second desalting washing liquid W2a toward the outside of the system. It may be directed to the liquid W5.
- the discharge to the elution tank 2 and / or the first solid-liquid separator 3 is discharged from the drain path provided in the first solid-liquid separator 3 via a predetermined valve mechanism Vd. It may be. Further, as will be described later, the drainage W5 may be discharged out of the system after being subjected to a heavy metal removal process.
- the chlorine-containing powder P1 and the first desalting washing liquid W1 are mixed and stirred to generate a slurry S1. At this time, the chlorine-containing powder P1 and the first desalting washing liquid W1 are generated.
- the mass ratio (W1 / P1) is preferably 4 to 10, more preferably 4 to 7, and particularly preferably 4 to 5. When the mass ratio (W1 / P1) is smaller than 4, elution of chlorine from the chlorine-containing powder P1 may be insufficient. Moreover, when mass ratio (W1 / P1) is larger than 10, the amount of the waste_water
- the chlorine ion concentration of the first desalting washing liquid W1 mixed with the chlorine-containing powder P1 in the elution tank 2 and constituting the slurry S1 is preferably 3% by mass to 15% by mass, and 3% by mass or more. 10% by mass is more preferable, and 3% by mass to 5% by mass is particularly preferable. That is, since water having a higher chlorine concentration than seawater can be used for the first desalting washing liquid W1, the chlorine concentration of the liquid phase discharged by solid-liquid separation of the slurry S1 in the subsequent step is 15% by mass or less.
- the liquid phase can be used as the first desalting washing liquid W1, and therefore the amount of waste water generated from the desalting treatment of the chlorine-containing powder can be effectively suppressed.
- the chlorine ion concentration of the first desalting washing liquid W1 exceeds the above range, the amount of chlorine eluted from the chlorine-containing powder P1 may be suppressed, and consequently the chlorine removal efficiency may be impaired.
- the lower limit of 3% by mass of the chlorine concentration of the first desalting washing liquid W1 is a value determined by using the seawater in the first desalting washing liquid W1.
- the pH of the slurry S1 is increased by seawater having an effect as a carbonate-based pH buffer solution. , Stabilized in a weak alkali range of 11-12.
- the stirring time of the slurry S1 by the stirring blade 24a is preferably 10 minutes to 3 hours, more preferably 10 minutes to 2 hours, and further preferably 15 minutes to 1 hour.
- the stirring time of the slurry S1 is shorter than 10 minutes, elution of chlorine from the chlorine-containing powder P1 may be insufficient.
- the stirring time of the slurry S1 is longer than 3 hours, the desalting amount of the chlorine-containing powder P1 per unit time is reduced.
- the elution tank 2 As the temperature condition for treating the slurry S1 in the elution tank 2, the higher the amount of chlorine eluted from the chlorine-containing powder P1, the higher the temperature, but from the viewpoint of processing costs, the room temperature range of 5 ° C to 30 ° C. Is preferable, and 15 ° C. to 30 ° C. is more preferable. In that case, the elution tank 2 may be provided with a predetermined temperature management device such as a heater.
- a general-purpose slurry pump such as a screw pump or a Mono pump may be used.
- the slurry S1 is separated into a first desalted cake C1 and a first filtrate W3.
- the salt content (C Cl (mass%)) in the separated first desalted cake C1 is the water content (C W (mass%)) of the first desalted cake C1
- the separated first Using the salt content (W Cl (mass%)) of the filtrate W3 and the water-insoluble salt content (C Cl-NS (mass%)) in the first desalted cake C1, the following formula (1) Can be approximated by C Cl ⁇ C W ⁇ W Cl + C Cl—NS (1)
- the water-insoluble salt content (C Cl—NS ) of the general chlorine-containing powder P1 is 0.8% by mass to 1.2% by mass.
- the first desalted cake C1 obtained by solid-liquid separation of the slurry S1 contains almost no chlorine. Since the liquid phase composed of a solid phase and a liquid phase in which chlorine is dissolved and contained in the first desalted cake C1 is the same as the first filtrate W3 separated by solid-liquid separation, the approximate expression ( Since 1) is established, in order to reduce the salt content (C Cl ) in the first desalted cake C1, the water content (C W ) of the first desalted cake C1 may be reduced.
- an apparatus capable of reducing the water content of the obtained first desalted cake C1 is used for the first solid-liquid separator 3, and a filter press is particularly preferably used as in this embodiment.
- the water content of the first desalted cake C1 obtained when the slurry S1 composed of the chlorine-containing powder P1 is solid-liquid separated by a filter press is usually 50% by mass or less.
- the first desalting cake C1 having a water content of about 50% by mass once obtained by solid-liquid separation is washed using the second desalting washing liquid W2. And substantially all of the liquid phase contained in the first desalting cake C1 is replaced with the second desalting washing liquid W2.
- the side surface of the desalted cake constituting the filter chamber constituting the filter chamber.
- the second desalting washing liquid W2 supplied from the second desalting washing liquid supply device 31 is press-fitted, and the second desalting washing liquid W2 is permeated through the first desalting cake C1.
- the liquid phase contained in the first desalting cake C1 is replaced with the second desalting washing liquid W2, which forms the second desalting cake C2. .
- This washing is performed while the water content of the desalted cake is about 50% by mass.
- the second desalting washing liquid W2 includes seawater, fresh water, or the second filtrate W4 when the second filtrate W4 is circulated, and any one of them, or What is necessary is just to use mixed water of those arbitrary combinations.
- the chlorine content of the second desalted cake C2 obtained by using the second desalting washing liquid W2 having a chlorine ion concentration of 3.5% by mass or less is set to at least the total wet mass of the cake. It can be 2% by mass or less.
- Even when fresh water is used for the second desalting washing liquid W2 the time for the second desalting washing liquid W2 to pass through the first desalting cake C1 in the above washing is relatively very high. Since it is a short time, unlike the elution step from the slurry, elution of the amphoteric metal component fixed to the solid phase of the first desalted cake C1 hardly occurs.
- the amount of the second desalting washing liquid W2 used in the desalting cake washing step is preferably 1 or more times the chlorine-containing powder P1 in the first desalting cake C1, more preferably 2 or more times, A 4-fold amount or more is particularly preferable.
- the amount of the second desalting washing liquid W2 used is less than one amount of the chlorine-containing powder P1, the liquid phase in the first desalting cake C1 having a water content of about 50% by mass is used as the second desalting salt. In some cases, the washing liquid W2 cannot be sufficiently replaced.
- cleaning liquid W2 exceeds 4 times amount of the chlorine containing powder P1, the amount of waste_water
- cleaning process increases.
- the confirmation that the liquid phase in the first desalting cake C1 has been switched to the second desalting washing liquid W2 is performed by monitoring the chlorine ion concentration of the second filtrate W4 discharged in the desalting cake washing process, What is necessary is just to confirm that the chlorine concentration is the same as or close to the chlorine ion concentration of the second desalting washing liquid W2.
- a general analysis method such as ion chromatography or a chlorine ion meter may be used directly from the second filtrate W4 or after preparing diluted water having an appropriate magnification.
- the first filtrate W ⁇ b> 3 and / or the second filtrate W ⁇ b> 4 from the first solid-liquid separation device 3 is supplied to the first desalting washing liquid supply device 22 by the first liquid feeding device 5.
- the first demineralization washing liquid W1 is circulated and used.
- the first desalting washing liquid W1 is based on circulation, and thereby the amount of process wastewater discharged is suppressed.
- the first filtrate W3 and / or the second filtrate W4 from the first solid-liquid separation device 3 is supplied to the first desalting washing liquid by the first liquid feeding device 5.
- the first desalting washing liquid W1 is basically circulated, but a part of the first desalting washing liquid W1 is supplied from the new first desalting washing liquid supply device 23 via the second supply regulating valve 23a.
- the fresh first desalting washing liquid W1a supplied to the 1 desalting washing supply apparatus 22 may be circulated and used while diluting the chlorine ion concentration.
- the timing and blending ratio at which a new first desalting washing solution W1a is added to one circulation may be set to a desired timing and blending ratio as appropriate based on the evaluation of the trial run.
- the first desalting washing liquid supply device 22 has a first supply adjustment composed of a predetermined adjustment valve mechanism that allows the contents of the reservoir to be discharged out of the system as the drainage W5.
- the valve 22a is provided, and the first filtrate W3 and the second filtrate W4 from the first solid-liquid separator 3 are discharged out of the system as a drainage W5 through a predetermined valve mechanism Vd. Is provided. Accordingly, the amount of the drainage liquid W5 directed to the outside of the system corresponding to the amount of the new first desalting washing liquid W1a added or the amount of the new second desalting washing liquid W2a added depending on the case.
- cleaning liquid W1 generally circulated and utilized can be adjusted suitably.
- the control device 201 receives a measurement signal from the first chlorine ion concentration monitoring device 7, and based on the measurement signal, sends a predetermined command signal to the first desalting washing liquid supply device.
- the first supply adjustment valve 22 a provided in the second supply adjustment valve 22 a, the second supply adjustment valve 23 a provided in the new first desalting washing liquid supply device 23, and the first liquid delivery device 5 can be transmitted. According to this, for example, when the measured value by the first chlorine ion concentration monitoring device 7 exceeds a predetermined threshold, the control device 201 transmits the command to the first liquid feeding device 5 based on the measurement result.
- the feeding of the first filtrate W3 and the second filtrate W4 due to the operation of the first liquid feeding device 5 is stopped, or these adjustments are made by command signals to the first supply regulating valve 22a and the second supply regulating valve 23a.
- Feedback control such as the valve mechanism performing the above-described operation to supply a new first desalting washing liquid W1a to the first desalting washing liquid W1 circulating in the system to perform a control to lower the chlorine ion concentration. It can be performed.
- a supply amount of a new first desalting washing liquid W1a corresponding to a measured value by the first chlorine ion concentration monitoring device 7 may be automatically determined, and the supply operation is automatically performed. It is also possible to make it continuous.
- control device 201 controls a predetermined valve mechanism to adjust the liquid amount (or slurry amount) of liquid feeding through the valve mechanism.
- the valve mechanism Vc may be controlled to control the feeding of the first filtrate W3 and the second filtrate W4 during the feedback control described above.
- the second desalted cake C2 discharged from the first solid-liquid separator 3 is transported to the cement manufacturing apparatus by the desalted cake transport device 9.
- the desalted cake transport device 9 is not particularly limited as long as it can transport a cake having a moisture content of about 50% by mass, and a general-purpose device such as a belt conveyor can be used.
- transportation means such as trucks and ships are adopted. It is also possible to do.
- FIG. 4 shows an overall configuration diagram showing a second embodiment of the chlorine-containing powder desalting apparatus according to the present invention.
- the second filtrate W4 discharged in the desalting cake washing process in the first solid-liquid separator 3. Is used as a second desalting washing solution. That is, the first filtrate W3 and / or the second filtrate W4 generated by the desalting cake forming step and / or the desalting cake washing step in the first solid-liquid separator 3 is a predetermined valve mechanism Ve.
- the first liquid delivery device 5 having a predetermined liquid delivery pump mechanism is used to send the liquid to the storage section of the first desalting washing liquid supply device 22 and circulate as the first desalting washing liquid W1.
- the second filtrate W4 discharged in the desalting cake washing process in the first solid-liquid separator 3 is supplied to a predetermined liquid feed pump mechanism via a predetermined valve mechanism Vf.
- the second liquid feeding device 6 is configured to be fed to the storage part of the second desalting washing liquid supply device 31 and can be circulated and used as the second desalting washing liquid W2. .
- a part or all of the second filtrate W4 is removed from the system via a predetermined valve mechanism Vc. It may be directed to the directed drainage W5.
- a second chlorine ion concentration monitoring device 8 is provided in the storage part of the second desalting washing liquid supply device 31, and the second desalting stored in the storage part of the second desalting washing liquid supply device 31.
- the chloride ion concentration of the salt washing liquid W2 is monitored.
- the second chlorine ion concentration monitoring device 8 may be the same as the first chlorine ion concentration monitoring device 7 described above.
- measurement is performed on diluted water having an appropriate magnification. Also good.
- a general-purpose analysis method such as a chlorine ion meter or ion chromatography may be used.
- a chlorine ion meter is used.
- the second chlorine ion concentration monitoring device 8 may be arranged such that the chlorine ion concentration of the contents in the reservoir of the second desalting washing liquid supply device 31 can be directly measured, or the second 2 may be disposed so as to be measurable at a position immediately before entering the storage section of the desalting washing liquid supply device 31, that is, in any arrangement, the chloride ion concentration in the second desalting washing liquid W2 may be determined. It only needs to be able to estimate.
- the second filtrate W4 from the first solid-liquid separation device 3 is sent to the storage part of the second desalting washing liquid supply device 31 by the second liquid feeding device 6, and It is designed to be circulated as 2 desalting washing liquid W2.
- the second desalting washing liquid W2 is based on the circulation use, and thereby the amount of process wastewater discharged is suppressed.
- the second desalting washing liquid W2 is basically circulated, but a part of the second desalting washing liquid W2 is supplied from the new second desalting washing liquid supply device 32 through the fourth supply regulating valve 32a.
- the timing and blending ratio at which a new second desalting washing liquid W2a is added to one circulation may be set to a desired timing and blending ratio as appropriate based on the evaluation of the trial run.
- the second desalting washing liquid supply device 31 has a third supply adjustment composed of a predetermined adjustment valve mechanism that allows the contents of the reservoir to be discharged out of the system as drainage W5.
- the valve 31a is provided, and the first filtrate W3 and / or the second filtrate W4 from the first solid-liquid separator 3 is directed out of the system as a drainage W5 through a predetermined valve mechanism Vc.
- a discharge route is provided. Accordingly, the amount of the drainage liquid W5 directed to the outside of the system in an amount corresponding to the amount of the new second desalting washing solution W2a added or the amount of the new first desalting washing solution W1a added in some cases. As a result, the range of the amount of the second desalting washing liquid W2 that is generally recycled and used can be adjusted as appropriate.
- the control device 201 is provided, and the second control is performed together with or independently of the feedback control by the first chlorine ion concentration monitoring device 7 described above.
- Feedback control by the chlorine ion concentration monitoring device 8 is enabled. That is, the measurement signal of the second chlorine ion concentration monitoring device 8 is received, and based on the measurement signal, a predetermined command signal is sent to the third supply adjustment valve 31a provided in the second desalting washing liquid supply device 31 or the new second Transmission to the fourth supply regulating valve 32 a provided in the desalting washing liquid supply device 32 or the second liquid feeding device 6 is enabled.
- the control device 201 transmits the command to the second liquid feeding device 6 based on the measurement result.
- the valve mechanism stops the liquid feeding of the second filtrate W4 due to the operation of the second liquid feeding device 6, or the valve mechanism performs the above-described operation according to the command signal to the third supply regulating valve 31a or the fourth supply regulating valve 32a.
- feedback control can be performed, for example, by supplying a new second desalting washing liquid W2a to the second desalting washing liquid W2 circulating in the system and performing a control to lower the chlorine ion concentration.
- a new supply amount of the second desalting washing liquid W2a corresponding to the measured value by the second chlorine ion concentration monitoring device 8 may be automatically determined. It is also possible to make it continuous.
- the control device 201 controls a predetermined valve mechanism to adjust the liquid amount (or slurry amount) of the liquid fed through the valve mechanism.
- the valve mechanism Ve may be controlled to control the feeding of the first filtrate W3 and the second filtrate W4 during the feedback control described above.
- the mechanism Vf may be controlled to control the feeding of the second filtrate W4 during the feedback control described above.
- FIGS. 5 to 9 are flowcharts showing still another embodiment of the chlorine-containing powder desalting method according to the present invention. In these embodiments, a treatment for removing heavy metals contained in the effluent generated by the desalting treatment according to the present invention is performed.
- FIG. 5 is a flowchart showing a third embodiment of the method for desalinating chlorine-containing powder according to the present invention.
- the second desalting washing liquid after circulation as the washing liquid it is reused as the first desalting washing liquid or the second desalting washing liquid.
- the heavy metal contained in the effluent produced by the desalting process according to the present invention can be separated and removed from the liquid phase of the effluent as a heavy metal agglomerated cake.
- the obtained heavy metal agglomerated cake can be effectively used as a cement raw material.
- the heavy metal scavenger include a combination of a pH adjuster and / or a redox potential adjuster and one or more flocculants such as an inorganic flocculant and a polymer flocculant.
- the redox potential (ORP) of the collected effluent is preferably ⁇ 200 mV or less, more preferably ⁇ 450 mV to ⁇ 200 mV.
- ORP redox potential
- a general-purpose one may be used as the oxidation-reduction potential adjusting agent.
- sodium hydrogen sulfide sodium hydrosulfide is preferable.
- an inorganic flocculant and an organic flocculant are used to make a heavy metal finely insolubilized by adjusting the oxidation-reduction potential into a larger flocculent floc form and facilitate separation from the liquid phase.
- the inorganic flocculant include iron chloride (FeCl 3 ) and polyaluminum chloride (PAC). Two or more of these may be used in combination.
- the amount of the inorganic flocculant added to the liquid phase is ascertained by the optimum addition amount based on the preliminary evaluation in the liquid to be treated. It is sufficient that the molar equivalent amount is about the same as the added amount.
- the organic flocculant is used for increasing the diameter of a small-diameter floc containing heavy metals formed of an inorganic flocculant.
- a flocculant used for solid-liquid separation in an alkaline region such as an anionic flocculant mainly composed of polyacrylamide may be used.
- the amount of the polymer flocculant added to the liquid phase is preferably the same as in the case of the amount of the inorganic flocculant added, but it is desirable to know the optimum addition amount based on the preliminary evaluation in the liquid to be treated. When evaluation is difficult, it is sufficient to add an amount of 20 to 30 ppm of the collected effluent.
- the pH of the collected effluent is preferably 7 to 11, more preferably 7.5 to 10.5, and the pH is 8 to 10.5. Is most preferred.
- the pH of the collected effluent is 7 to 11, heavy metals can be effectively insolubilized.
- the pH of the recovered effluent and the removal rate of Pb from the effluent As an example of the relationship, when the pH is 6, the Pb removal rate is 84.2%, when the pH is 12, the Pb removal rate is 98.9%, and when the pH is 10.5, the Pb removal rate is 99.
- recovered waste liquid a general purpose thing may be used, for example, what is necessary is just to use general purpose pH adjusters, such as a sulfuric acid and sodium hydroxide.
- the pH of the recovered effluent is adjusted with a pH adjuster as necessary, and a redox potential adjuster is added and stirred for 5 to 20 minutes.
- a redox potential adjuster is added and stirred for 5 to 20 minutes.
- an inorganic flocculant is added and stirred and mixed for 5 to 20 minutes, and a polymer flocculant is further added and stirred and mixed for 5 to 20 minutes.
- the insolubilized heavy metal has a larger-diameter aggregated floc form, while chlorine is dissolved at a high concentration in the liquid phase, and the aggregated floc containing heavy metal is suspended in the liquid phase.
- the aggregation floc containing liquid of such a structure usually makes a slurry form.
- the liquid from the agglomerated floc-containing liquid containing the insolubilized heavy metal is obtained using a solid-liquid separation means such as a filter press in the same manner as used in the desalting treatment of the chlorine-containing powder. A part or all of the phases are separated to obtain a heavy metal agglomerated cake (first agglomerated cake) and a third filtrate.
- FIG. 6 is a flowchart showing a fourth embodiment of the method for desalinating chlorine-containing powder according to the present invention.
- a heavy metal agglomerated cake washing step is provided, the first agglomerated cake is washed with the third desalting washing liquid, and the washed heavy metal agglomerated cake (hereinafter, Also referred to as “second agglomerated cake”) and a fourth filtrate.
- second agglomerated cake also referred to as “second agglomerated cake”
- the 2nd aggregation cake from which chlorine was fully removed can be obtained, and it is easy to use it more suitably as a cement raw material.
- FIG. 7 is a flow chart showing a fifth embodiment of the method for desalinating chlorine-containing powder according to the present invention.
- the fourth filtrate obtained in the heavy metal agglomerated cake washing step is at least partly a first desalting washing solution used for the desalting treatment described above.
- cleaning liquid can be reduced.
- FIG. 8 is a flowchart showing a sixth embodiment of the method for desalinating chlorine-containing powder according to the present invention.
- at least a part of the second filtrate obtained in the desalting cake washing step in the desalting treatment described above is the second filtrate for washing the heavy metal agglomerated cake.
- the cleaning treatment in the heavy metal agglomerated cake cleaning step is performed while controlling the chlorine ion concentration of the third desalting cleaning solution by using as the 3 desalting cleaning solution. Thereby, the usage-amount of the wash water utilized as a 3rd desalting washing
- the chlorine ion concentration of the third desalting washing liquid tends to increase, and consequently the chlorine ions remaining in the second agglomerated cake.
- the concentration tends to increase. For example, if it is used as it is, it tends to be difficult to use it as a cement raw material.
- the treatment is performed while controlling the chlorine ion concentration of the third desalting washing solution, the third desalting washing is performed. When the chlorine ion concentration of the liquid becomes unsuitable for processing, it can be corrected at an appropriate timing.
- FIG. 9 is a flow chart showing a seventh embodiment of the method for desalinating chlorine-containing powder according to the present invention.
- the fourth filtrate obtained in the heavy metal agglomerated cake washing step circulates and uses at least a part thereof as the third desalting washing solution.
- the washing process in the heavy metal agglomerated cake washing step is performed while controlling the chlorine ion concentration of the third desalting washing solution. Thereby, the usage-amount of the wash water utilized as a 3rd desalting washing
- the chlorine ion concentration of the third desalting washing liquid tends to increase, and as a result, the chlorine remaining in the second agglomerated cake.
- the ion concentration tends to increase. For example, if it is used as it is, it tends to be difficult to use it as a cement raw material.
- the treatment is performed while controlling the chlorine ion concentration of the third desalting washing solution, When the chlorine ion concentration of the washing liquid becomes unsuitable for treatment, it can be corrected at an appropriate timing.
- the third desalting wash used in the present invention is the same as the first desalting wash and the second desalting wash used in the desalting treatment described above, such as the use of seawater. It is. However, when the third desalting washing solution is circulated and used, the chlorine ion concentration of the third desalting washing solution for washing the desalted cake at the first iteration is 3.5% by mass or less. It is preferably 3% by mass or less, and most preferably 2.5% by mass or less. The same applies to the chlorine ion concentration of the third desalting washing liquid for washing the desalted cake after a plurality of repeated treatments.
- chlorine ion concentration exceeds the above range, chlorine ions remain in a high concentration in the desalted cake obtained after the heavy metal agglomerated cake washing step, and as a result, it cannot be used as a cement raw material as it is. It is.
- the third desalting is performed. Since the chlorine ion concentration of the washing liquid rises according to the number of repetitions of the circulating use of the second filtrate in the desalting treatment described above, this is monitored and controlled. Moreover, since the chlorine ion concentration of the 3rd desalting washing
- “monitoring” and “control” have the same meaning as in the case of the first desalting washing liquid and the second desalting washing liquid in the desalting treatment described above.
- the “third desalting washing liquid” as an object of “monitoring” or “control” is not only directly monitoring or controlling the state of washing the first agglomerated cake, but also a predetermined blending ratio.
- the chlorine ion concentration of that before the preparation may be targeted. That is, the chlorine ion concentration of the third desalting washing liquid constituting the washing liquid for washing the first agglomerated cake may be substantially monitored and controlled.
- the chlorine ion concentration of the third desalting washing solution that goes around the system increases excessively, and chlorine ions remain in a high concentration in the second agglomerated cake obtained after washing the first agglomerated cake, As a result, it is possible to prevent the use as a cement raw material from being difficult as it is.
- the chlorine ion concentration of the third desalting washing liquid for washing the first agglomerated cake exceeds a predetermined threshold value
- the chlorine ion concentration of the third desalting washing liquid circulating in the system is set. What is necessary is just to process for every chlorine containing powder supplied after adjusting arbitrarily or washing
- FIG. 10 is an overall configuration diagram showing a third embodiment of the chlorine-containing powder demineralization apparatus according to the present invention.
- the desalting apparatus 20 includes a heavy metal insolubilization reaction tank 11, and the first filtrate, the second filtrate, and the first desalted washing liquid in the desalting process described above are used after circulation.
- the first desalting washing liquid Alternatively, what is not reused as the second desalting washing liquid can be collected and stored as drainage.
- the first filtrate W3 and / or the second filtrate W4 are discharged from the solid-liquid separation device 3 in the desalting process described above via a predetermined valve mechanism Vd.
- the liquid W5 is directed toward the outside of the system, it can be recovered and stored in the heavy metal insolubilization reaction tank 11.
- the first desalting washing liquid that is not used again from the reservoir of the first desalting washing liquid supply device 22 in the desalting treatment described above is further supplied via the first supply regulating valve 22a to a predetermined valve mechanism.
- the waste liquid W5 is directed toward the outside of the system via Vg and Vh, it can be recovered and stored in the heavy metal insolubilization reaction tank 11.
- the second desalting washing liquid that is not used again from the storage part of the second desalting washing liquid supply device 31 in the desalting treatment described above is further supplied to the predetermined valve mechanism via the first supply regulating valve 31a.
- the waste liquid W5 is directed toward the outside of the system via Vi and Vh, it can be recovered and stored in the heavy metal insolubilization reaction tank 11. Further, as described above, in the desalting process described above, the discharge of the contents of the storage portion of the first desalting washing liquid supply device 22 and / or the second desalting washing liquid supply device 31 toward the outside of the system is performed.
- a predetermined valve mechanism Vd is provided from the drainage path provided in the solid-liquid separation device 3 so as to be routed to the elution tank 2 and the solid-liquid separation device 3. Therefore, such waste liquid W5 can also be collected and stored in the heavy metal insolubilization reaction tank 11.
- the heavy metal insolubilization reaction tank 11 is provided with the ORP regulator supply device 111, and the heavy metal insolubilization reaction tank 11 can be appropriately supplied with the oxidation-reduction potential regulator A1.
- the inorganic flocculant supply apparatus 112 is provided, and the inorganic flocculant A2 can be appropriately supplied to the heavy metal insolubilization reaction tank 11.
- the polymer flocculant supply apparatus 113 is provided, and the polymer flocculant A3 can be appropriately supplied to the heavy metal insolubilization reaction tank 11.
- the pH adjuster supply device 114 is provided, and the pH adjuster A4 can be appropriately supplied to the heavy metal insolubilization reaction tank 11.
- the heavy metal insolubilization reaction tank 11 is provided with a stirring device 115, and by rotating the stirring blade 115a, the storage in the tank can be mixed and stirred for a predetermined time.
- a heavy metal scavenger such as a redox potential adjuster, an inorganic flocculant, or a polymer flocculant is added to the collected effluent, and preferably the redox potential adjuster as described above. Then, an inorganic flocculant and a polymer flocculant are added in this order to insolubilize the heavy metal in the drained liquid in the form of agglomerated flocs to form a slurry-like agglomerated floc-containing liquid (hereinafter referred to as “slurry S2”). .
- slurry S2 slurry-like agglomerated floc-containing liquid
- the stirring blade 115a of the stirring device 115 by rotating the stirring blade 115a of the stirring device 115, the waste liquid W5 composed of the first filtrate W3 or the second filtrate W4, the oxidation-reduction potential adjusting agent A1, Inorganic flocculant A2, polymer flocculant A3, and pH adjuster A4 can be mixed and stirred for a predetermined time to form slurry S2.
- the stirring time for forming the slurry S2 by the stirring blade 115a is preferably 5 minutes to 20 minutes, more preferably 10 minutes for each addition of the oxidation-reduction potential adjusting agent, the inorganic flocculant, and the polymer flocculant. -20 minutes, more preferably 15-20 minutes.
- the temperature condition for treating the slurry S2 in the heavy metal insolubilization reaction tank 11 is not particularly limited, and a normal temperature range of 5 ° C. to 30 ° C. is preferable, and 15 ° C. to 30 ° C. is more preferable from the viewpoint of processing costs.
- the heavy metal insolubilization reaction tank 11 is provided with a redox potential monitoring device 161 to monitor the redox potential of the collected waste liquid stored in the heavy metal insolubilization reaction tank 11.
- a redox potential monitoring device 161 to monitor the redox potential of the collected waste liquid stored in the heavy metal insolubilization reaction tank 11.
- a known measuring device may be used.
- a measuring device for high concentration suspension may be used.
- the heavy metal insolubilization reaction tank 11 is provided with a pH monitoring device 164 to monitor the pH of the collected waste liquid stored in the heavy metal insolubilization reaction tank 11.
- a pH monitoring device 164 a known measuring device may be used, and the same measuring device as the oxidation-reduction potential monitoring device 161 may be used as long as the oxidation-reduction potential can be measured.
- the ORP regulator supply apparatus 111 is provided with an ORP regulator supply regulation valve 111 a composed of a predetermined regulation valve mechanism, and is supplied from the ORP regulator supply apparatus 111 to the heavy metal insolubilization reaction tank 11. It is possible to adjust the supply amount of the oxidation-reduction potential adjusting agent A1.
- the inorganic flocculant supply device 112 is provided with an inorganic flocculant supply adjustment valve 112a having a predetermined adjustment valve mechanism, and the amount of inorganic flocculant A2 supplied from the inorganic flocculant supply device 112 to the heavy metal insolubilization reaction tank 11 is supplied.
- the polymer flocculant supply device 113 is provided with a polymer flocculant supply adjustment valve 113a having a predetermined adjustment valve mechanism, and the heavy metal insolubilization reaction tank is provided from the polymer flocculant supply device 113.
- 11 is capable of adjusting the supply amount of the polymer flocculant A3 supplied to 11
- the pH adjuster supply device 114 is provided with a pH adjuster supply adjusting valve 114a including a predetermined adjusting valve mechanism.
- the supply amount of the pH adjuster A4 supplied from the pH adjuster supply device 114 to the heavy metal insolubilization reaction tank 11 can be adjusted.
- a control device 201 that can function in common with feedback control of the chlorine ion concentration in the desalting process described above is provided.
- the control device 201 further includes a redox potential monitoring device 161.
- the measurement result and the measurement result of the pH monitoring device 164 are transmitted at any time.
- the command to the ORP regulator supply regulating valve 111a is transmitted by the control device 201 based on the measurement result.
- feedback control can be performed, such as control for lowering the oxidation-reduction potential by supplying the oxidation-reduction potential adjusting agent A1 to the reaction tank 11.
- the command signal to the pH adjuster supply adjustment valve 114a that the control device 201 transmits based on the measurement result can be performed, for example, by controlling the pH by supplying the pH adjuster A4 to the reaction tank 11.
- a second solid-liquid separation device 13 that separates the slurry S2 discharged from the heavy metal insolubilization reaction tank 11 and conveyed by the slurry conveyance device 12 is provided.
- the second solid-liquid separator 13 a part or all of the liquid phase is separated from the slurry S2 to obtain a heavy metal agglomerated cake (hereinafter referred to as “first agglomerated cake C3”) and a third filtrate W6.
- first agglomerated cake C3 heavy metal agglomerated cake
- W6 third filtrate W6.
- the filter press etc. which were used as the 1st solid-liquid separator 3 in the above-mentioned desalting process.
- general purpose slurry pumps such as a screw pump and a Mono pump, as the slurry conveyance apparatus 12.
- the first agglomerated cake C3 discharged from the second solid-liquid separator 13 is conveyed to the cement manufacturing apparatus by the heavy metal agglomerated cake conveying device 15.
- the heavy metal agglomerated cake transport device 15 is the same as the desalted cake transport device 9 used in the desalting process described above, and is particularly limited as long as it can transport a cake having a moisture content of about 50% by mass.
- a general-purpose device such as a belt conveyor can be used.
- transportation means such as trucks and ships are adopted. It is also possible to do.
- FIG. 11 is an overall configuration diagram showing a fourth embodiment of the chlorine-containing powder desalting apparatus according to the present invention.
- the first agglomerated cake C3 is used for the third desalting. Washing with the third desalting washing liquid W7 supplied from the washing liquid supply apparatus 141 is enabled.
- a valve mechanism Vj is provided in the middle of the path for conveying the slurry S2 treated in the heavy metal insolubilization reaction tank 11 to the second solid-liquid separator 13, while the third desalting washing liquid supply device.
- Another valve mechanism Vk is also provided in the middle of the path through which the third desalting washing liquid W3 flows from the 141 to the second solid-liquid separator 13, and the slurry S2 and the third desalting washing liquid W7 are selected.
- the second solid-liquid separation device 13 can be directed to the second solid-liquid separation device 13, and the slurry S2 is first directed to the second solid-liquid separation device 13 and processed by the second solid-liquid separation device 13 to produce the first agglomerated cake C3.
- the third desalting washing liquid W3 is directed to the second solid-liquid separator 13 to wash the first agglomerated cake C3 to obtain the second agglomerated cake C4 and the fourth filtrate W8. To be able to.
- the third filtrate W6 generated by the heavy metal agglomerated cake forming step and the fourth filtrate W8 generated by the heavy metal agglomerated cake washing step are a predetermined valve mechanism. It can be discharged out of the system as drainage W9 through Vl.
- the fourth filtrate W8 obtained by the heavy metal agglomerated cake washing step is passed through a predetermined valve mechanism Vm by a third liquid feeding device 16 including a predetermined liquid feeding pump mechanism. The liquid is sent to the reservoir of the first desalting washing liquid supply device 22 so that it can be circulated and used as the first desalting washing liquid W1.
- the third desalting washing liquid supply device 141 is provided with a fifth supply regulating valve 141 a having a predetermined regulating valve mechanism, and is provided in the third desalting washing liquid supply device 141. Whether the contents in the storage tank are directed to the second solid-liquid separator 13 as the third desalting washing liquid W7 or the waste liquid W9 directed to the outside of the system is distributed by the fifth supply regulating valve 141a. It is possible to adjust the amount of liquid directed to them. Further, a new third desalting washing liquid supply device 142 for supplying a new third desalting washing liquid W7a to the third desalting washing liquid supply device 141 is provided.
- the sixth supply regulating valve 142a is added as part of the third desalting washing liquid in the system, or a third desalting washing liquid repeatedly used a plurality of times, if desired. Part or all can be exchanged.
- the content of the storage part of the third desalting washing liquid supply device 141 is appropriately discharged in accordance with the amount of the new third desalting washing liquid W7a supplied to the outside of the system. It may be directed to the liquid W9.
- the second solid-liquid separation device 13 is at a desired timing such as a timing at which the slurry S2 is not processed.
- the liquid may be discharged from the liquid discharge path provided in the second solid-liquid separator 13 via a predetermined valve mechanism Vl.
- the embodiment shown in FIG. 11 is provided with a control device 201 that can function in common with the feedback control of the chlorine ion concentration in the desalting process described above and further in the feedback control in the embodiment described with reference to FIG.
- the control device 201 receives the measurement signal from the first chlorine ion concentration monitoring device 7 and, based on the measurement signal, can also transmit the third liquid feeding device 16. According to this, for example, when the measured value by the first chlorine ion concentration monitoring device 7 exceeds a predetermined threshold, the control device 201 transmits the command to the third liquid feeding device 16 based on the measurement result.
- the operation of the third liquid supply device 16 is stopped by the signal, or the operation of the adjustment valve mechanism described above by the command signal to the first supply adjustment valve 22a or the second supply adjustment valve 23a is stopped. So that feedback control can be performed, for example, by supplying a new first desalting washing liquid W1a to the first desalting washing liquid W1 circulating in the system to lower the chlorine ion concentration. I have to.
- a supply amount of a new first desalting washing liquid W1a corresponding to a measured value by the first chlorine ion concentration monitoring device 7 may be automatically determined, and the supply operation is automatically performed. It is also possible to make it continuous.
- control device 201 controls the valve mechanism to adjust the liquid amount (or slurry amount) of the liquid fed through the valve mechanism. Accordingly, for example, the valve mechanism Vm may be controlled to control the feeding of the fourth filtrate W8 during the feedback control described above.
- FIG. 12 is an overall configuration diagram showing a fifth embodiment of the chlorine-containing powder demineralization apparatus according to the present invention.
- the desalting apparatus 40 according to this embodiment includes the second filtrate W4 generated by the desalting cake washing step in the desalting process described above.
- a path for feeding liquid to the storage part of the third desalting washing liquid supply apparatus 141 is provided by the fourth liquid feeding apparatus 17 including a predetermined liquid feeding pump mechanism via the predetermined valve mechanism Vn. It can also be used as the salt washing liquid W7.
- the fourth filtrate W8 generated in the heavy metal agglomerated cake washing step is subjected to the third desalting washing by the fifth liquid feeding device 18 including a predetermined liquid feeding pump mechanism via the predetermined valve mechanism Vo.
- a path for feeding the liquid to the storage part of the liquid supply apparatus 141 is provided so that it can be circulated and used as the third desalting washing liquid W7.
- a third chlorine ion concentration monitoring device 19 is provided in the storage section of the third desalting washing liquid supply apparatus 141, and the storage section of the third desalting washing liquid supply apparatus 141.
- the chlorine ion concentration of the third desalting washing liquid W7 stored in the tank is monitored.
- the third chlorine ion concentration monitoring device 19 may be the same as the first chlorine ion concentration monitoring device 7 and the second chlorine ion concentration monitoring device 8 described above, and is suitable for measuring the chlorine ion concentration. You may measure about the dilution water of magnification.
- a general-purpose analysis method such as a chlorine ion meter or ion chromatography may be used.
- a chlorine ion meter is used.
- the chlorine ion concentration of the contents in the storage part of the third desalting washing liquid supply device 141 may be arranged so as to be directly measurable, or the second It may be arranged to be measurable at a position immediately before entering the storage section of the 3 desalting washing liquid supply device 141, that is, in any arrangement, the chlorine ion concentration in the third desalting washing liquid W7 It only needs to be able to estimate.
- control device 201 that can function in common with the feedback control of the chlorine ion concentration in the desalting process described above, and further in the feedback control in the embodiment described with reference to FIGS.
- the control device 201 further receives a measurement signal from the third chlorine ion concentration monitoring device 19, and can transmit it to the fourth liquid feeding device 17 and the fifth liquid feeding device 18 based on the measurement signal. I have to. According to this, for example, when the measured value by the third chlorine ion concentration monitoring device 19 exceeds a predetermined threshold value, the fourth liquid feeding device 17 and / or the control device 201 transmits based on the measurement result.
- the feeding of the second filtrate W4 by the operation of the fourth liquid feeding device 17 is stopped by the command signal to the fifth liquid feeding device 18, or the fourth filtrate W8 is fed by the operation of the fifth liquid feeding device 18.
- the control valve mechanism performs the above-described operation in response to a command signal to the fifth supply adjustment valve 141a or the sixth supply adjustment valve 142a, and a new desalting washing liquid W7 circulating in the system is added.
- Feedback control can be performed, for example, by supplying the third desalting washing liquid W7a to control to lower the chlorine ion concentration.
- a supply amount of a new third desalting washing liquid W7a corresponding to the measurement value by the third chlorine ion concentration monitoring device 19 may be automatically determined, and the supply operation is automatically performed. It is also possible to make it continuous.
- the control device 201 controls a predetermined valve mechanism and adjusts the liquid amount (or slurry amount) of the liquid fed through the valve mechanism.
- the valve mechanism Vn may be controlled to control the feeding of the second filtrate W4 during the feedback control described above.
- the valve mechanism Vo may be controlled to control the feeding of the fourth filtrate W8 during the feedback control described above.
- FIG. 13 shows a chlorine-containing powder desalination treatment method and chlorine-containing powder desorption provided by the present invention in accordance with the configuration of the chlorine-containing powder desalination apparatus shown in FIG.
- FIG. 2 is an overall configuration flowchart showing the salt treatment apparatus in a more explanatory manner.
- it is needless to say that a part of the configuration shown in FIG. 13 can be omitted as appropriate within the range described above.
- FIG. 14 shows a desalting apparatus 50 in which the first solid-liquid separation device and the second solid-liquid separation device are the same device.
- FIG. 15 is a flowchart showing the overall configuration according to the embodiment.
- the structure, function, etc. represented by the explanatory notes and symbols shown in FIGS. 14 and 15 are the same as those in FIGS. 10 to 13 described above.
- the solid-liquid separation apparatus to be used can be made common and the apparatus configuration can be simplified.
- Table 1 shows how the salt concentration of each washing solution affects the treatment of the molten fly ash P1 in the treatment of the molten fly ash P1 by the configuration of the chlorine-containing powder desalination treatment apparatus 1 shown in FIG.
- the molten fly ash of level A shown in Table 1 the first desalting washing liquid W1 having the salinity levels shown in Table 2 and the second desalting washing having the salinity levels shown in Table 3
- the liquid W2 was used in the combinations shown in Table 4, and the molten fly ash P1 was processed and evaluated.
- the solid-liquid ratio of slurry S1 (the mass ratio of “first desalting washing liquid W1 / molten fly ash P1”) is 4, and stirring of slurry S1 is performed by rotating stirring blade 24a of stirring device 24.
- the water content of the first desalted cake C1 and the second desalted cake C2 obtained by stirring at several 400 rpm for 30 minutes and the treatment in the first solid-liquid separator 3 is 50% by mass, depending on the second desalting washing liquid W2.
- the second desalted cake C2 at the time of washing is subjected to the treatment of the molten fly ash P1 under various conditions such that the solid-liquid ratio (mass ratio of “second desalting washing liquid W2 / molten fly ash P1”) is 1. It was.
- a filter press was used as the first solid-liquid separator 3.
- the Cl concentration, the Pb concentration and the Zn concentration of the first filtrate W3 obtained by solid-liquid separation of the liquid phase derived from the first desalting washing solution W1 are determined according to JIS K 0102 “ The test was carried out in accordance with “Factory drainage test method”. Specifically, potentiometric titration was used for Cl concentration, and ICP mass spectrometry was used for Pb concentration and Zn concentration (device used: Agilent 7900 ICP-MS (trade name) manufactured by Agilent Technologies).
- the chlorine content of the second desalted cake C2 after being washed with the second desalting washing solution W2 was measured using a potentiometric titration method after the sample was decomposed with nitric acid and hydrogen peroxide. The results are shown in Table 5.
- the Cl concentration of the second desalted cake C2 after washing with the second desalting washing liquid W2 was 2.0% by mass or less.
- the slurry S1 was stirred for 30 minutes Thereafter, the Pb concentration and the Zn concentration of the first filtrate W3 obtained by solid-liquid separation of the liquid phase derived from the first desalting washing liquid W1 showed a low value of 1 ppm or less.
- Test Example 1-11 and Test Example 1-12 in which the molten fly ash P1 was mixed with high chlorine concentration water having a chlorine concentration of 18% by mass as the first desalting washing solution W1, the high fly Elution of chlorine from the molten fly ash P1 into the chlorine-concentrated water was not sufficient, and the Cl concentration of the second desalted cake C2 could not be reduced sufficiently.
- the ORP regulator NaSH
- the ORP regulator NaSH
- the mixture was stirred for 15 minutes, and then the same amount of the inorganic flocculant (FeCl 3 ) as that of the ORP regulator was added for 15 minutes. Stir. Thereafter, 30 ppm of a polymer flocculant (Diafloc, manufactured by Mitsubishi Chemical Corporation) was added.
- the treated effluent thus obtained was subjected to solid-liquid separation by suction filtration to obtain a system effluent W9 (corresponding to the third filtrate W6) at each pH.
- Table 6 shows the amount of heavy metal components of the drainage liquid W5 (reference example) directed outside the system before pH adjustment and the system drainage liquid W9 (corresponding to the third filtrate W6) at each pH. In addition, Table 6 shows the uniform drainage standard values in Japan.
- Chlorine-containing powder desalting apparatus Elution tank 3 First solid-liquid separation apparatus 4, 12 Slurry conveying apparatus 5 First liquid feeding apparatus (pump mechanism) 6 Second liquid feeding device (pump mechanism) 7 First chlorine ion concentration monitoring device 8 Second chlorine ion concentration monitoring device 9 Desalted cake transport device 11 Heavy metal insolubilization reaction tank 15 Heavy metal agglomerated cake transport device 16 Third liquid feeding device (pump mechanism) 17 4th liquid feeding device (pump mechanism) 18 Fifth liquid feeding device (pump mechanism) 19 Third chlorine ion concentration monitoring device 21 Chlorine-containing powder supply device 22 First washing water supply device for desalting 22a First supply regulating valve (regulating valve mechanism) 23 New first desalting washing liquid supply device 23a Second supply regulating valve (regulating valve mechanism) 24, 115 Stirring device 24a, 115a Stirring blade 31 Second desalting washing liquid supply device 31a Third supply regulating valve (regulating valve mechanism) 32 New second desalting washing liquid supply device 32a Fourth supply regulating valve (regulating valve mechanism) 111 OR
Abstract
Description
塩素含有粉体に第1脱塩用洗液を混合してスラリーにするスラリー化工程と、
前記スラリー中で前記塩素含有粉体に含まれる塩素を液相中に溶出させる塩素溶出工程と、
前記塩素を溶出させた該スラリーから液相の一部又は全部を分離して第1脱塩ケーキと第1ろ液を得る脱塩ケーキ形成工程と、
前記第1脱塩ケーキを、前記第1脱塩用洗液とは別個の第2脱塩用洗液で洗浄して第2脱塩ケーキと第2ろ液を得る脱塩ケーキ洗浄工程とを備え、
前記脱塩ケーキ形成工程で得られる前記第1ろ液、及び/又は前記脱塩ケーキ洗浄工程で得られる前記第2ろ液は、少なくともその一部を前記第1脱塩用洗液として循環利用して、前記第1脱塩用洗液の塩素イオン濃度を制御しつつ、前記スラリー化工程と、前記塩素溶出工程と、前記脱塩ケーキ形成工程と、前記脱塩ケーキ洗浄工程とを、供給される塩素含有粉体ごとに繰り返すことを特徴とする塩素含有粉体の脱塩処理方法を提供するものである。
(1)前記第1ろ液、前記第2ろ液、前記第1脱塩用洗液として循環利用後の該第1脱塩用洗液、及び前記第2脱塩用洗液として循環利用後の該第2脱塩用洗液からなる群から選ばれた1種又は2種以上のうち、前記第1脱塩用洗液又は前記第2脱塩用洗液として再度利用しないものを排液として回収する排液回収工程
(2)前記工程(1)で回収した排液に重金属捕集剤を添加して、該排液に含まれる重金属を凝集フロック状に不溶化する重金属不溶化工程
(3)前記工程(2)で不溶化した重金属を含む凝集フロック含有液から液相の一部又は全部を分離して第1凝集ケーキと第3ろ液を得る重金属凝集ケーキ形成工程
(4)前記第1凝集ケーキを、前記第1脱塩用洗液及び前記第2脱塩用洗液とは別個の第3脱塩用洗液で洗浄して第2凝集ケーキと第4ろ液を得る重金属凝集ケーキ洗浄工程
第1脱塩用洗液を供給するための第1脱塩用洗液供給装置と、
塩素含有粉体を前記第1脱塩用洗液供給装置からの前記第1脱塩用洗液と混合してスラリーにするとともに、前記スラリー中で前記塩素含有粉体に含まれる塩素を液相中に溶出させるための溶出槽と、
前記塩素を溶出させた該スラリーから液相の一部又は全部を分離して第1脱塩ケーキと第1ろ液を得る処理を行なう第1固液分離装置と、
前記溶出槽で処理された前記スラリーを前記第1固液分離装置に搬送するためのスラリー搬送装置と、
前記第1固液分離装置において、前記第1脱塩用洗液とは別個の第2脱塩用洗液で前記第1脱塩ケーキを洗浄して第2脱塩ケーキと第2ろ液を得る処理を行なうよう、その第2脱塩用洗液を供給するための第2脱塩用洗液供給装置と、
前記第1固液分離装置でなされる前記第1脱塩ケーキの形成処理で得られる前記第1ろ液、及び/又は前記第1固液分離装置でなされる前記第1脱塩ケーキの洗浄処理で得られる前記第2ろ液を、少なくともその一部を前記第1脱塩用洗液として循環利用するため、前記第1脱塩用洗液供給装置に送液するための第1送液装置と、
前記第1脱塩用洗液の塩素イオン濃度を監視するための第1塩素イオン濃度監視装置を備えたことを特徴とする塩素含有粉体の脱塩処理装置を提供するものである。
前記塩素含有粉体の脱塩処理装置は、更に、前記第1脱塩用洗液供給装置に前記第1脱塩用洗液として新たな第1脱塩用洗液を供給するための新たな第1脱塩用洗液の供給装置を備え、
前記第1脱塩用洗液供給装置は、該第1脱塩用洗液供給装置から前記溶出槽への前記第1脱塩用洗液の供給量を可変可能にするとともに、該第1脱塩用洗液供給装置から排液することを可能にする第1供給調整弁を備え、
前記新たな第1脱塩用洗液の供給装置は、前記第1脱塩用洗液供給装置への該洗液の供給量を可変可能にする第2供給調整弁を備え、
前記第1脱塩用洗液の塩素イオン濃度が第1閾値を超えた場合、前記第1供給調整弁を制御することにより、前記第1脱塩用洗液供給装置からの前記第1脱塩用洗液の前記溶出槽への供給を止め又は減少させ、前記第1脱塩用洗液供給装置から前記第1脱塩用洗液の一部又は全部を排液したうえ、前記新たな第1脱塩用洗液の供給装置の前記第2供給調整弁を制御することにより、前記第1脱塩用洗液供給装置に、前記第1脱塩用洗液として前記第1閾値を満足するように前記新たな第1脱塩用洗液を供給するように構成された、該脱塩処理装置を提供するものである。
前記第1固液分離装置でなされる前記第1脱塩ケーキの洗浄処理で得られる前記第2ろ液を、少なくともその一部を前記第2脱塩用洗液として循環利用するため、前記第2脱塩用洗液供給装置に送液するための第2送液装置と、
前記第2脱塩用洗液の塩素イオン濃度を監視するための第2塩素イオン濃度監視装置とを備える、該脱塩処理装置を提供するものである。
前記塩素含有粉体の脱塩処理装置は、更に、前記第2脱塩用洗液供給装置に前記第2脱塩用洗液として新たな第2脱塩用洗液を供給するための新たな第2脱塩用洗液の供給装置を備え、
前記第2脱塩用洗液供給装置は、該第2脱塩用洗液供給装置から前記第1脱塩ケーキへの前記第2脱塩用洗液の供給量を可変可能にするとともに、該第2脱塩用洗液供給装置から排液することを可能にする第3供給調整弁を備え、
前記新たな第2脱塩用洗液の供給装置は、前記第2脱塩用洗液供給装置への該洗液の供給量を可変可能にする第4供給調整弁を備え、
前記第2脱塩用洗液の塩素イオン濃度が前記第1閾値とは別個の第2閾値を超えた場合、前記第3供給調整弁を制御することにより、前記第2脱塩用洗液供給装置からの前記第2脱塩用洗液の前記第1脱塩ケーキへの供給を止め又は減少させ、前記第2脱塩用洗液供給装置から前記第2脱塩用洗液の一部又は全部を排液したうえ、前記新たな第2脱塩用洗液の供給装置の前記第4供給調整弁を制御することにより、前記第2脱塩用洗液供給装置に、前記第2脱塩用洗液として前記第2閾値を満足するように前記新たな第2脱塩用洗液を供給するように構成された、該脱塩処理装置を提供するものである。
前記第1ろ液及び前記第2ろ液のうち、前記第1脱塩用洗液又は前記第2脱塩用洗液として再度利用しないもの、前記第1脱塩用洗液供給装置から排液として送液された前記第1脱塩用洗液、及び前記第2脱塩用洗液供給装置から排液として送液された前記第2脱塩用洗液からなる群から選ばれた1種又は2種以上を排液として回収して収容し、これに重金属捕集剤を添加することにより、該排液に含まれる重金属を凝集フロック状に不溶化させるための重金属不溶化反応槽と、
前記不溶化した重金属を含む凝集フロック含有液から液相の一部又は全部を分離して第1凝集ケーキと第3ろ液を得る処理を行なう第2固液分離装置と、
前記重金属不溶化反応槽で処理された前記凝集フロック含有液を前記第2固液分離装置に搬送するための凝集フロック含有液搬送装置とを備える、該脱塩処理装置を提供するものである。
前記第2固液分離装置において、前記第1脱塩用洗液及び前記第2脱塩用洗液とは別個の第3脱塩用洗液で洗浄して第2凝集ケーキと第4ろ液を得る処理を行なうよう、その第3脱塩用洗液を供給するための第3脱塩用洗液供給装置を備える、該脱塩処理装置を提供するものである。
前記第2固液分離装置でなされる前記第1凝集ケーキの洗浄処理で得られる前記第4ろ液を、少なくともその一部を前記第1脱塩用洗液として循環利用するため、前記第1脱塩用洗液供給装置に送液するための第3送液装置を備える、該脱塩処理装置を提供するものである。
前記第1固液分離装置でなされる前記第1脱塩ケーキの洗浄処理で得られる前記第2ろ液を、少なくともその一部を前記第3脱塩用洗液として利用するため、前記第3脱塩用洗液供給装置に送液するための第4送液装置と、及び/又は、
前記第2固液分離装置でなされる前記第1凝集ケーキの洗浄処理で得られる前記第4ろ液を、少なくともその一部を前記第3脱塩用洗液として循環利用するため、前記第3脱塩用洗液供給装置に送液するための第5送液装置と、
前記第3脱塩用洗液の塩素イオン濃度を監視するための第3塩素イオン濃度監視装置とを備える、該脱塩処理装置を提供するものである。
前記第3脱塩用洗液供給装置は、該第3脱塩用洗液供給装置から前記第1凝集ケーキへの前記第3脱塩用洗液の供給量を可変可能にするとともに、該第3脱塩用洗液供給装置から排液することを可能にする第5供給調整弁を備え、
前記新たな第3脱塩用洗液の供給装置は、前記第3脱塩用洗液供給装置への該洗液の供給量を可変可能にする第6供給調整弁を備え、
前記第3脱塩用洗液の塩素イオン濃度が前記第1閾値及び前記第2閾値とは別個の第3閾値を超えた場合、前記第5供給調整弁を制御することにより、前記第3脱塩用洗液供給装置からの前記第3脱塩用洗液の前記第1凝集ケーキへの供給を止め又は減少させ、前記第3脱塩用洗液供給装置から前記第3脱塩用洗液の一部又は全部を排液したうえ、前記新たな第3脱塩用洗液の供給装置の前記第6供給調整弁を制御することにより、前記第3脱塩用洗液供給装置に、前記第3脱塩用洗液として前記第3閾値を満足するように前記新たな第3脱塩用洗液を供給するように構成された、該脱塩処理装置を提供するものである。
CCl≒CW×WCl+CCl-NS・・・(1)
ここで、一般的な塩素含有粉体P1の非水溶性塩分含有率(CCl-NS)は、0.8質量%~1.2質量%である。
結果を表5に示す。
2 溶出槽
3 第1固液分離装置
4、12 スラリー搬送装置
5 第1送液装置(ポンプ機構)
6 第2送液装置(ポンプ機構)
7 第1塩素イオン濃度監視装置
8 第2塩素イオン濃度監視装置
9 脱塩ケーキ搬送装置
11 重金属不溶化反応槽
15 重金属凝集ケーキ搬送装置
16 第3送液装置(ポンプ機構)
17 第4送液装置(ポンプ機構)
18 第5送液装置(ポンプ機構)
19 第3塩素イオン濃度監視装置
21 塩素含有粉体供給装置
22 第1脱塩用洗液供給装置
22a 第1供給調整弁(調整弁機構)
23 新たな第1脱塩用洗液の供給装置
23a 第2供給調整弁(調整弁機構)
24、115 撹拌装置
24a、115a 撹拌翼
31 第2脱塩用洗液供給装置
31a 第3供給調整弁(調整弁機構)
32 新たな第2脱塩用洗液の供給装置
32a 第4供給調整弁(調整弁機構)
111 ORP調整剤供給装置
111a ORP調整剤供給調整弁
112 無機凝集剤供給装置
112a 無機凝集剤供給調整弁
113 高分子凝集剤供給装置
113a 高分子凝集剤供給調整弁
114 pH調整剤供給装置
114a pH調整剤供給調整弁
141 第3脱塩用洗液供給装置
141a 第5供給調整弁(調整弁機構)
142 新たな第1脱塩用洗液の供給装置
142a 第6供給調整弁(調整弁機構)
201 制御装置
Va~Vo バルブ機構
P1 塩素含有粉体
S1、S2 スラリー
C1 第1脱塩ケーキ
C2 第2脱塩ケーキ
C3 第1凝集ケーキ
C4 第2凝集ケーキ
W1 第1脱塩用洗液
W1a 新たな第1脱塩用洗液
W2 第2脱塩用洗液
W2a 新たな第2脱塩用洗液
W3 第1ろ液
W4 第2ろ液
W5 系外に向けた排液
W6 第3ろ液
W7 第3脱塩用洗液
W7a 新たな第3脱塩用洗液
W8 第4ろ液
W9 系外排液
Claims (24)
- 塩素含有粉体に第1脱塩用洗液を混合してスラリーにするスラリー化工程と、
前記スラリー中で前記塩素含有粉体に含まれる塩素を液相中に溶出させる塩素溶出工程と、
前記塩素を溶出させた該スラリーから液相の一部又は全部を分離して第1脱塩ケーキと第1ろ液を得る脱塩ケーキ形成工程と、
前記第1脱塩ケーキを、前記第1脱塩用洗液とは別個の第2脱塩用洗液で洗浄して第2脱塩ケーキと第2ろ液を得る脱塩ケーキ洗浄工程とを備え、
前記脱塩ケーキ形成工程で得られる前記第1ろ液、及び/又は前記脱塩ケーキ洗浄工程で得られる前記第2ろ液は、少なくともその一部を前記第1脱塩用洗液として循環利用して、前記第1脱塩用洗液の塩素イオン濃度を制御しつつ、前記スラリー化工程と、前記塩素溶出工程と、前記脱塩ケーキ形成工程と、前記脱塩ケーキ洗浄工程とを、供給される塩素含有粉体ごとに繰り返すことを特徴とする塩素含有粉体の脱塩処理方法。 - 前記第1脱塩用洗液の塩素イオン濃度が第1閾値を超えた場合、前記第1脱塩用洗液を、新たな第1脱塩用洗液により前記第1閾値を満足するように制御する、請求項1に記載の塩素含有粉体の脱塩処理方法。
- 前記塩素含有粉体に加える初回の第1脱塩用洗液として海水を利用し、前記第1脱塩用洗液の塩素イオン濃度が15質量%を超えないようにする、請求項1に記載の塩素含有粉体の脱塩処理方法。
- 前記脱塩ケーキ洗浄工程で得られる前記第2ろ液は、少なくともその一部を前記第2脱塩用洗液として循環利用して、前記第2脱塩用洗液の塩素イオン濃度を制御しつつ、前記スラリー化工程と、前記塩素溶出工程と、前記脱塩ケーキ形成工程と、前記脱塩ケーキ洗浄工程とを、供給される塩素含有粉体ごとに繰り返す、請求項1に記載の塩素含有粉体の脱塩処理方法。
- 前記第2脱塩用洗液の塩素イオン濃度が前記第1閾値とは別個の第2閾値を超えた場合、前記第2脱塩用洗液を、新たな第2脱塩用洗液により前記第2閾値を満足するように制御する、請求項4に記載の塩素含有粉体の脱塩処理方法。
- 前記第2脱塩用洗液の塩素イオン濃度が3.5質量%を超えないようにする、請求項4又は5に記載の塩素含有粉体の脱塩処理方法。
- 更に下記(1)~(3)の工程を備える、請求項1に記載の塩素含有粉体の脱塩処理方法。
(1)前記第1ろ液、前記第2ろ液、前記第1脱塩用洗液として循環利用後の該第1脱塩用洗液、及び前記第2脱塩用洗液として循環利用後の該第2脱塩用洗液からなる群から選ばれた1種又は2種以上のうち、前記第1脱塩用洗液又は前記第2脱塩用洗液として再度利用しないものを排液として回収する排液回収工程
(2)前記工程(1)で回収した排液に重金属捕集剤を添加して、該排液に含まれる重金属を凝集フロック状に不溶化する重金属不溶化工程
(3)前記工程(2)で不溶化した重金属を含む凝集フロック含有液から液相の一部又は全部を分離して第1凝集ケーキと第3ろ液を得る重金属凝集ケーキ形成工程 - 更に下記(4)の工程を備える、請求項7記載の塩素含有粉体の脱塩処理方法。
(4)前記第1凝集ケーキを、前記第1脱塩用洗液及び前記第2脱塩用洗液とは別個の第3脱塩用洗液で洗浄して第2凝集ケーキと第4ろ液を得る重金属凝集ケーキ洗浄工程 - 前記重金属不溶化工程は、前記排液のpHを7~11とする、請求項7又は8に記載の塩素含有粉体の脱塩処理方法。
- 前記重金属凝集ケーキ洗浄工程で得られる前記第4ろ液は、少なくともその一部を前記第1脱塩用洗液として循環利用する、請求項8に記載の塩素含有粉体の脱塩処理方法。
- 前記脱塩ケーキ洗浄工程で得られる前記第2ろ液は、少なくともその一部を前記第3脱塩用洗液として利用し、及び/又は前記重金属凝集ケーキ洗浄工程で得られる前記第4ろ液は、少なくともその一部を前記第3脱塩用洗液として循環利用し、前記第3脱塩用洗液の塩素イオン濃度を制御しつつ、前記重金属凝集ケーキ洗浄工程における洗浄処理を行う、請求項10に記載の塩素含有粉体の脱塩処理方法。
- 前記第3脱塩用洗液の塩素イオン濃度が前記第1閾値及び前記第2閾値とは別個の第3閾値を超えた場合、前記第3脱塩用洗液を、新たな第3脱塩用洗液により前記第3閾値を満足するように制御する、請求項11に記載の塩素含有粉体の脱塩処理方法。
- 前記第3脱塩用洗液の塩素イオン濃度が3.5質量%を超えないようにする、請求項11に記載の塩素含有粉体の脱塩処理方法。
- 前記塩素含有粉体が、焼却飛灰、溶融飛灰、及び塩素バイパスダストから選ばれた1種又は2種以上を含むものである、請求項1又は7に記載の塩素含有粉体の脱塩処理方法。
- 第1脱塩用洗液を供給するための第1脱塩用洗液供給装置と、
塩素含有粉体を前記第1脱塩用洗液供給装置からの前記第1脱塩用洗液と混合してスラリーにするとともに、前記スラリー中で前記塩素含有粉体に含まれる塩素を液相中に溶出させるための溶出槽と、
前記塩素を溶出させた該スラリーから液相の一部又は全部を分離して第1脱塩ケーキと第1ろ液を得る処理を行なう第1固液分離装置と、
前記溶出槽で処理された前記スラリーを前記第1固液分離装置に搬送するためのスラリー搬送装置と、
前記第1固液分離装置において、前記第1脱塩用洗液とは別個の第2脱塩用洗液で前記第1脱塩ケーキを洗浄して第2脱塩ケーキと第2ろ液を得る処理を行なうよう、その第2脱塩用洗液を供給するための第2脱塩用洗液供給装置と、
前記第1固液分離装置でなされる前記第1脱塩ケーキの形成処理で得られる前記第1ろ液、及び/又は前記第1固液分離装置でなされる前記第1脱塩ケーキの洗浄処理で得られる前記第2ろ液を、少なくともその一部を前記第1脱塩用洗液として循環利用するため、前記第1脱塩用洗液供給装置に送液するための第1送液装置と、
前記第1脱塩用洗液の塩素イオン濃度を監視するための第1塩素イオン濃度監視装置を備えたことを特徴とする塩素含有粉体の脱塩処理装置。 - 前記塩素含有粉体の脱塩処理装置は、更に、前記第1脱塩用洗液供給装置に前記第1脱塩用洗液として新たな第1脱塩用洗液を供給するための新たな第1脱塩用洗液の供給装置を備え、
前記第1脱塩用洗液供給装置は、該第1脱塩用洗液供給装置から前記溶出槽への前記第1脱塩用洗液の供給量を可変可能にするとともに、該第1脱塩用洗液供給装置から排液することを可能にする第1供給調整弁を備え、
前記新たな第1脱塩用洗液の供給装置は、前記第1脱塩用洗液供給装置への該洗液の供給量を可変可能にする第2供給調整弁を備え、
前記第1脱塩用洗液の塩素イオン濃度が第1閾値を超えた場合、前記第1供給調整弁を制御することにより、前記第1脱塩用洗液供給装置からの前記第1脱塩用洗液の前記溶出槽への供給を止め又は減少させ、前記第1脱塩用洗液供給装置から前記第1脱塩用洗液の一部又は全部を排液したうえ、前記新たな第1脱塩用洗液の供給装置の前記第2供給調整弁を制御することにより、前記第1脱塩用洗液供給装置に、前記第1脱塩用洗液として前記第1閾値を満足するように前記新たな第1脱塩用洗液を供給するように構成された、請求項15に記載の塩素含有粉体の脱塩処理装置。 - 前記塩素含有粉体の脱塩処理装置は、更に、
前記第1固液分離装置でなされる前記第1脱塩ケーキの洗浄処理で得られる前記第2ろ液を、少なくともその一部を前記第2脱塩用洗液として循環利用するため、前記第2脱塩用洗液供給装置に送液するための第2送液装置と、
前記第2脱塩用洗液の塩素イオン濃度を監視するための第2塩素イオン濃度監視装置とを備える、請求項15に記載の塩素含有粉体の脱塩処理装置。 - 前記塩素含有粉体の脱塩処理装置は、更に、前記第2脱塩用洗液供給装置に前記第2脱塩用洗液として新たな第2脱塩用洗液を供給するための新たな第2脱塩用洗液の供給装置を備え、
前記第2脱塩用洗液供給装置は、該第2脱塩用洗液供給装置から前記第1脱塩ケーキへの前記第2脱塩用洗液の供給量を可変可能にするとともに、該第2脱塩用洗液供給装置から排液することを可能にする第3供給調整弁を備え、
前記新たな第2脱塩用洗液の供給装置は、前記第2脱塩用洗液供給装置への該洗液の供給量を可変可能にする第4供給調整弁を備え、
前記第2脱塩用洗液の塩素イオン濃度が前記第1閾値とは別個の第2閾値を超えた場合、前記第3供給調整弁を制御することにより、前記第2脱塩用洗液供給装置からの前記第2脱塩用洗液の前記第1脱塩ケーキへの供給を止め又は減少させ、前記第2脱塩用洗液供給装置から前記第2脱塩用洗液の一部又は全部を排液したうえ、前記新たな第2脱塩用洗液の供給装置の前記第4供給調整弁を制御することにより、前記第2脱塩用洗液供給装置に、前記第2脱塩用洗液として前記第2閾値を満足するように前記新たな第2脱塩用洗液を供給するように構成された、請求項17に記載の塩素含有粉体の脱塩処理装置。 - 前記塩素含有粉体の脱塩処理装置は、更に、
前記第1ろ液及び前記第2ろ液のうち、前記第1脱塩用洗液又は前記第2脱塩用洗液として再度利用しないもの、前記第1脱塩用洗液供給装置から排液として送液された前記第1脱塩用洗液、及び前記第2脱塩用洗液供給装置から排液として送液された前記第2脱塩用洗液からなる群から選ばれた1種又は2種以上を排液として回収して収容し、これに重金属捕集剤を添加することにより、該排液に含まれる重金属を凝集フロック状に不溶化させるための重金属不溶化反応槽と、
前記不溶化した重金属を含む凝集フロック含有液から液相の一部又は全部を分離して第1凝集ケーキと第3ろ液を得る処理を行なう第2固液分離装置と、
前記重金属不溶化反応槽で処理された前記凝集フロック含有液を前記第2固液分離装置に搬送するための凝集フロック含有液搬送装置とを備える、請求項15又は17に記載の塩素含有粉体の脱塩処理装置。 - 前記塩素含有粉体の脱塩処理装置は、更に、
前記第2固液分離装置において、前記第1脱塩用洗液及び前記第2脱塩用洗液とは別個の第3脱塩用洗液で洗浄して第2凝集ケーキと第4ろ液を得る処理を行なうよう、その第3脱塩用洗液を供給するための第3脱塩用洗液供給装置を備える、請求項19に記載の塩素含有粉体の脱塩処理装置。 - 前記塩素含有粉体の脱塩処理装置は、更に、
前記第2固液分離装置でなされる前記第1凝集ケーキの洗浄処理で得られる前記第4ろ液を、少なくともその一部を前記第1脱塩用洗液として循環利用するため、前記第1脱塩用洗液供給装置に送液するための第3送液装置を備える、請求項19に記載の塩素含有粉体の脱塩処理装置。 - 前記塩素含有粉体の脱塩処理装置は、更に、
前記第1固液分離装置でなされる前記第1脱塩ケーキの洗浄処理で得られる前記第2ろ液を、少なくともその一部を前記第3脱塩用洗液として利用するため、前記第3脱塩用洗液供給装置に送液するための第4送液装置と、及び/又は、
前記第2固液分離装置でなされる前記第1凝集ケーキの洗浄処理で得られる前記第4ろ液を、少なくともその一部を前記第3脱塩用洗液として循環利用するため、前記第3脱塩用洗液供給装置に送液するための第5送液装置と、
前記第3脱塩用洗液の塩素イオン濃度を監視するための第3塩素イオン濃度監視装置とを備える、請求項19に記載の塩素含有粉体の脱塩処理装置。 - 前記塩素含有粉体の脱塩処理装置は、更に、前記第3脱塩用洗液供給装置に前記第3脱塩用洗液として新たな第3脱塩用洗液を供給するための新たな第3脱塩用洗液の供給装置を備え、
前記第3脱塩用洗液供給装置は、該第3脱塩用洗液供給装置から前記第1凝集ケーキへの前記第3脱塩用洗液の供給量を可変可能にするとともに、該第3脱塩用洗液供給装置から排液することを可能にする第5供給調整弁を備え、
前記新たな第3脱塩用洗液の供給装置は、前記第3脱塩用洗液供給装置への該洗液の供給量を可変可能にする第6供給調整弁を備え、
前記第3脱塩用洗液の塩素イオン濃度が前記第1閾値及び前記第2閾値とは別個の第3閾値を超えた場合、前記第5供給調整弁を制御することにより、前記第3脱塩用洗液供給装置からの前記第3脱塩用洗液の前記第1凝集ケーキへの供給を止め又は減少させ、前記第3脱塩用洗液供給装置から前記第3脱塩用洗液の一部又は全部を排液したうえ、前記新たな第3脱塩用洗液の供給装置の前記第6供給調整弁を制御することにより、前記第3脱塩用洗液供給装置に、前記第3脱塩用洗液として前記第3閾値を満足するように前記新たな第3脱塩用洗液を供給するように構成された、請求項22に記載の塩素含有粉体の脱塩処理装置。 - 前記第1固液分離装置と前記第2固液分離装置とは、同一の装置でそれぞれによる処理を行う、請求項19に記載の塩素含有粉体の脱塩処理装置。
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