CN104386662B - A kind of method utilizing phosphatization waste residue to produce tricalcium phosphate co-production ferric oxide - Google Patents
A kind of method utilizing phosphatization waste residue to produce tricalcium phosphate co-production ferric oxide Download PDFInfo
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Abstract
The present invention relates to phosphatization waste reside comprehensive utilization technical field, especially a kind of method utilizing phosphatization waste residue to produce tricalcium phosphate co-production ferric oxide, by phosphatization waste residue is adopted oxygenant pre-treatment step, and then make the ferro element in phosphatization waste residue can be oxidized to ferric ion completely, and then carry out alkalinisation treatment, ferro element wherein is comparatively comprehensively removed, and then the extraction yield that improve in phosphatization waste residue reaches more than 99.13%, reduce the content of the ferro element in phosphatization waste residue simultaneously, and then according to enrichment principle, the concentration of phosphate radical is wherein improved, and then add calcium chloride raw material wherein again, and then the calcium ion in phosphate radical and calcium chloride is reacted, and control temperature and pH value, and then the output of calcium phosphate is improved, extract phosphoric to greatest extent, and make the purity of tricalcium phosphate reach more than 98.1%.
Description
Technical field
The present invention relates to phosphatization waste reside comprehensive utilization technical field, especially a kind of method utilizing phosphatization waste residue to produce tricalcium phosphate co-production ferric oxide.
Background technology
Phosphatization waste residue is a kind of white waste residue of solid, in the complete processings such as various metal insert, antitheft door, by a large amount of waste produced after phosphating process, can be divided into common phosphatization waste residue and Zinc phosphating waste residue etc. according to the different ions composition wherein contained, therefore in phosphatization waste residue, main component is the existence of ferro element and phosphate radical or hydrogen phosphate.And the current method for phosphatization Solid state fermentation is all adopt landfill and directly send into building field to carry out the production decocting material, and then a large amount of phosphatization waste residues is processed; In above-mentioned treatment process, landfill not only can bring contaminate environment largely, and physical environment is destroyed, but also natural resources can be caused to suffer serious loss, makes the chemical resource such as phosphoric, ferro element be wasted in physical environment; Although phosphatization waste residue is used for building field by the pollution for the treatment of process reduction to environment, still can cause the waste of the chemical resource such as phosphoric, ferro element, simultaneously when processing, process added value also can be caused lower, and cost is higher; There is investigator by fully utilizing phosphatization waste residue for this reason, tertiary iron phosphate in phosphatization waste residue is carried out the method extracting application, but directly from phosphatization waste residue, extract tertiary iron phosphate, not only can cause and the extraction difficulty of tertiary iron phosphate is strengthened, in leaching process, also can add other material, not the material element product added is extracted, and then make the processing cost of phosphatization waste residue larger, added value is lower, and then makes the further integrated application sight of phosphatization waste residue poor.
For this reason, this researchist is by understanding the characteristic of phosphatization waste residue, and then the ferro element in phosphatization waste residue and phosphoric are fully utilized, and the starting material added all can be formed product and extract, and again the waste residue processed is used for building field, improve the comprehensive utilization value of phosphatization waste residue, produce highly purified tricalcium phosphate product, the Application Areas again for phosphatization waste residue provides a kind of new selection.
Summary of the invention
In order to solve the above-mentioned technical problem existed in prior art, the invention provides a kind of method utilizing phosphatization waste residue to produce tricalcium phosphate co-production ferric oxide, have and the ferro element in phosphatization waste residue is extracted to greatest extent, make the concentration of residual phosphate radical in the solution larger, and then add calcium chloride raw material wherein again, and then make phosphate radical and this ion form calcium phosphate, and then the phosphate radical in phosphatization waste residue is extracted, improve phosphatization waste reside comprehensive utilization rate, reduce the feature of comprehensive utilization cost.
Be achieved particular by following technical scheme:
Utilize phosphatization waste residue to produce a method for tricalcium phosphate co-production ferric oxide, comprise the following steps:
(1) phosphatization waste residue pre-treatment: phosphatization waste residue is placed in pulverizer and is ground into 100-120 object powder, again powder is placed in pretreatment pool, be (2-3) according to powder with the proportioning of oxidizing acid: 1 mixes, during mixing, oxidizing acid is added in pretreatment pool, and the stirring velocity that employing stirring speed is 30-50r/min carries out stir process, after property to be oxidized acid has added, after Keep agitation speed stirs 30-50min, adjustment temperature is 30-55 DEG C, leave standstill 20-40min, add the 2-3 water doubly of powder weight more wherein, and to adjust stirring velocity be 100-120r/min, after Keep agitation 30-60min, stop stirring, and carried out filtration treatment, obtain filter residue and filtrate, filter residue is transported to Building Materials Factory and produces building materials, filtrate gives over to stand-by,
(2) alkalize: by step 1) filtrate that obtains proceeds in alkalization pond, and limit adds sodium hydroxide limit and takes stirring velocity to be 40-50r/min stir process wherein, temperature in adjustment alkalization pond is 70-80 DEG C, when having a large amount of reddish-brown precipitations to occur in extremely alkalization pond to be added, adjustment stirring velocity is 100-130r/min, and after continuing to add phosphatization waste residue weight 0.4-0.9 sodium hydroxide doubly wherein, Keep agitation 10-20min, stop stir process, and adjust temperature be at 50-70 DEG C leave standstill, stand-by;
(3) be separated: by step 2) in the solution containing precipitation be placed in separating machine, carry out solid-liquid separation process, obtain solid and liquid, wherein solid is placed in drying machine, after adopting the temperature drying treatment 10-30s of 90-100 DEG C, acquisition ferric oxide; Liquid is stand-by;
(4) heat: by step 3) obtain liquid be placed in well heater, heat-up rate is adopted to be 1 DEG C/min hyperthermic treatment, and when hyperthermic treatment, add calcium chloride solution wherein, treat that the pH value of solution reaches 10-12.1, stop adding of calcium chloride solution, employing stirring speed is after 60-90r/min stir process 20-30min, stop hyperthermic treatment, and to adjust temperature is after 60-70 DEG C, carried out filtration treatment, obtained solid phase and liquid phase; Solid phase is placed in drying machine and adopts the dry 30-40s of the temperature of 90 DEG C, obtains tricalcium phosphate; Liquid phase is stand-by;
(5) cooling: by step 4) liquid phase that obtains is placed in water cooler and carries out cooling process to after 0-5 DEG C, be placed on again in separating machine and carry out separating treatment, obtain waste liquid and precipitation, calcium chloride dissolution process is carried out in waste back-cycling calcium chloride dissolving tank, precipitation adopts clear water to be after 1:3 mixes according to precipitating with the mass ratio of clear water, employing stirring speed is after 40-60r/min stir process 10-20min, and after being warming up to 20-30 DEG C, be placed on again in separator and carry out filtration treatment, obtain liquid phase A and solid phase A, solid phase A is placed in after calcium chloride dissolving tank dissolves once again, add step 4 again) in, liquid phase A is placed in cooling crystallizer and carries out the process of repetition crystallisation by cooling, repeat crystallisation by cooling process and reduce temperature to≤3 DEG C, after leaving standstill cooling process 20-50min, filtered, obtain waste liquid A and solid A, waste liquid A returns the dissolving carrying out calcium chloride in calcium chloride dissolving tank again, solid A is placed in drying machine, after adopting the dry 30-50s of the temperature of 70-80 DEG C, obtain sodium-chlor product, can complete and adopt phosphatization waste residue to produce tricalcium phosphate.
The solution of described sodium hydroxide to be mass percent be 30-70%.
Described oxidizing acid is hypochlorous acid, also can adopt hydrogen peroxide.
Described calcium chloride solution adopts water to dissolve calcium chloride in calcium chloride dissolving tank, and then formulated mass percent is the solution of 50-70%.
Compared with prior art, technique effect of the present invention is embodied in:
1. by phosphatization waste residue is adopted oxygenant pre-treatment step, and then make the ferro element in phosphatization waste residue can be oxidized to ferric ion completely, and then carry out alkalinisation treatment, ferro element wherein is comparatively comprehensively removed, and then the extraction yield that improve in phosphatization waste residue reaches more than 99.13%, reduce the content of the ferro element in phosphatization waste residue simultaneously, and then according to enrichment principle, the concentration of phosphate radical is wherein improved, and then add calcium chloride raw material wherein again, and then the calcium ion in phosphate radical and calcium chloride is reacted, and control temperature and pH value, and then the output of calcium phosphate is improved, extract phosphoric to greatest extent, and make the purity of tricalcium phosphate reach more than 98.1%.
2. the waste residue after process is also used for building field by the present invention, and then not only make ferro element wherein and phosphoric resource obtain maximized application, also make waste residue can not be emitted in physical environment, and then avoid the pollution of environment, and after preparing calcium phosphate, again by the chlorion added in solution, sodium ion further extracts, and then reduce the waste of industrial chemicals, reduce the cost that phosphatization waste reside comprehensive utilization produces tricalcium phosphate product, and during the waste back-cycling calcium chloride emitted is dissolved, and then the discharging of waste liquid amount avoided in whole technique, reduce environmental, there is significant economic benefit and the value of environmental protection.
Embodiment
Below in conjunction with concrete embodiment, further restriction is done to technical scheme of the present invention, but claimed scope is not only confined to done description.
Embodiment 1
Utilize phosphatization waste residue to produce a method for tricalcium phosphate co-production ferric oxide, comprise the following steps:
(1) phosphatization waste residue pre-treatment: phosphatization waste residue is placed in pulverizer and is ground into 100 object powder, again powder is placed in pretreatment pool, be that 2:1 mixes according to powder and the proportioning of oxidizing acid, during mixing, oxidizing acid is added in pretreatment pool, and the stirring velocity that employing stirring speed is 30r/min carries out stir process, after property to be oxidized acid has added, after Keep agitation speed stirs 30min, adjustment temperature is 30 DEG C, leave standstill 20min, add the water of 2 times of powder weight more wherein, and to adjust stirring velocity be 100r/min, after Keep agitation 30min, stop stirring, and carried out filtration treatment, obtain filter residue and filtrate, filter residue is transported to Building Materials Factory and produces building materials, filtrate gives over to stand-by,
(2) alkalize: by step 1) filtrate that obtains proceeds in alkalization pond, and limit adds sodium hydroxide limit and takes stirring velocity to be 40r/min stir process wherein, temperature in adjustment alkalization pond is 70 DEG C, when having a large amount of reddish-brown precipitations to occur in extremely alkalization pond to be added, adjustment stirring velocity is 100r/min, and after continuing to add the sodium hydroxide of phosphatization waste residue weight 0.4 times wherein, Keep agitation 10min, stop stir process, and adjust temperature be at 50 DEG C leave standstill, stand-by;
(3) be separated: by step 2) in the solution containing precipitation be placed in separating machine, carry out solid-liquid separation process, obtain solid and liquid, wherein solid is placed in drying machine, after adopting the temperature drying treatment 10s of 90 DEG C, acquisition ferric oxide; Liquid is stand-by;
(4) heat: by step 3) obtain liquid be placed in well heater, heat-up rate is adopted to be 1 DEG C/min hyperthermic treatment, and when hyperthermic treatment, add calcium chloride solution wherein, treat that the pH value of solution reaches 10, stop adding of calcium chloride solution, employing stirring speed is after 60r/min stir process 20min, stop hyperthermic treatment, and to adjust temperature is after 60 DEG C, carried out filtration treatment, obtained solid phase and liquid phase; Solid phase is placed in drying machine and adopts the dry 30s of the temperature of 90 DEG C, obtains tricalcium phosphate; Liquid phase is stand-by;
(5) cooling: by step 4) liquid phase that obtains is placed in after water cooler carries out cooling process to 0 DEG C, be placed on again in separating machine and carry out separating treatment, obtain waste liquid and precipitation, calcium chloride dissolution process is carried out in waste back-cycling calcium chloride dissolving tank, precipitation adopts clear water to be after 1:3 mixes according to precipitating with the mass ratio of clear water, employing stirring speed is after 40r/min stir process 10min, and after being warming up to 20 DEG C, be placed on again in separator and carry out filtration treatment, obtain liquid phase A and solid phase A, solid phase A is placed in after calcium chloride dissolving tank dissolves once again, add step 4 again) in, liquid phase A is placed in cooling crystallizer and carries out the process of repetition crystallisation by cooling, repeat crystallisation by cooling process and reduce temperature to 2 DEG C, after leaving standstill cooling process 20min, filtered, obtain waste liquid A and solid A, waste liquid A returns the dissolving carrying out calcium chloride in calcium chloride dissolving tank again, solid A is placed in drying machine, after adopting the dry 30s of the temperature of 70 DEG C, obtain sodium-chlor product, can complete and adopt phosphatization waste residue to produce tricalcium phosphate.
Described sodium hydroxide to be mass percent be 30% solution.
Described oxidizing acid is hypochlorous acid.
Described calcium chloride solution adopts water to dissolve calcium chloride in calcium chloride dissolving tank, and then formulated mass percent is the solution of 50%.
Measure the rate of recovery of ferro element: can learn that the pick-up rate of ferric oxide is 99.13%;
Measure the purity of tricalcium phosphate, can learn, the purity of tricalcium phosphate is 98.13%.
Embodiment 2
Utilize phosphatization waste residue to produce a method for tricalcium phosphate co-production ferric oxide, comprise the following steps:
(1) phosphatization waste residue pre-treatment: phosphatization waste residue is placed in pulverizer and is ground into 120 object powder, again powder is placed in pretreatment pool, be that 3:1 mixes according to powder and the proportioning of oxidizing acid, during mixing, oxidizing acid is added in pretreatment pool, and the stirring velocity that employing stirring speed is 50r/min carries out stir process, after property to be oxidized acid has added, after Keep agitation speed stirs 50min, adjustment temperature is 55 DEG C, leave standstill 40min, add the water of 3 times of powder weight more wherein, and to adjust stirring velocity be 120r/min, after Keep agitation 60min, stop stirring, and carried out filtration treatment, obtain filter residue and filtrate, filter residue is transported to Building Materials Factory and produces building materials, filtrate gives over to stand-by,
(2) alkalize: by step 1) filtrate that obtains proceeds in alkalization pond, and limit adds sodium hydroxide limit and takes stirring velocity to be 50r/min stir process wherein, temperature in adjustment alkalization pond is 80 DEG C, when having a large amount of reddish-brown precipitations to occur in extremely alkalization pond to be added, adjustment stirring velocity is 130r/min, and after continuing to add the sodium hydroxide of phosphatization waste residue weight 0.9 times wherein, Keep agitation 20min, stop stir process, and adjust temperature be at 70 DEG C leave standstill, stand-by;
(3) be separated: by step 2) in the solution containing precipitation be placed in separating machine, carry out solid-liquid separation process, obtain solid and liquid, wherein solid is placed in drying machine, after adopting the temperature drying treatment 30s of 100 DEG C, acquisition ferric oxide; Liquid is stand-by;
(4) heat: by step 3) obtain liquid be placed in well heater, heat-up rate is adopted to be 1 DEG C/min hyperthermic treatment, and when hyperthermic treatment, add calcium chloride solution wherein, treat that the pH value of solution reaches 12.1, stop adding of calcium chloride solution, employing stirring speed is after 90r/min stir process 30min, stop hyperthermic treatment, and to adjust temperature is after 70 DEG C, carried out filtration treatment, obtained solid phase and liquid phase; Solid phase is placed in drying machine and adopts the dry 40s of the temperature of 90 DEG C, obtains tricalcium phosphate; Liquid phase is stand-by;
(5) cooling: by step 4) liquid phase that obtains is placed in after water cooler carries out cooling process to 5 DEG C, be placed on again in separating machine and carry out separating treatment, obtain waste liquid and precipitation, calcium chloride dissolution process is carried out in waste back-cycling calcium chloride dissolving tank, precipitation adopts clear water to be after 1:3 mixes according to precipitating with the mass ratio of clear water, employing stirring speed is after 60r/min stir process 20min, and after being warming up to 30 DEG C, be placed on again in separator and carry out filtration treatment, obtain liquid phase A and solid phase A, solid phase A is placed in after calcium chloride dissolving tank dissolves once again, add step 4 again) in, liquid phase A is placed in cooling crystallizer and carries out the process of repetition crystallisation by cooling, repeat crystallisation by cooling process and reduce temperature to 3 DEG C, after leaving standstill cooling process 50min, filtered, obtain waste liquid A and solid A, waste liquid A returns the dissolving carrying out calcium chloride in calcium chloride dissolving tank again, solid A is placed in drying machine, after adopting the dry 50s of the temperature of 80 DEG C, obtain sodium-chlor product, can complete and adopt phosphatization waste residue to produce tricalcium phosphate.
Described sodium hydroxide to be mass percent be 70% solution.
Described oxidizing acid is hydrogen peroxide.
Described calcium chloride solution adopts water to dissolve calcium chloride in calcium chloride dissolving tank, and then formulated mass percent is the solution of 70%.
Measure the rate of recovery of ferro element: can learn that the pick-up rate of ferric oxide is 99.17%;
Measure the purity of tricalcium phosphate, can learn, the purity of tricalcium phosphate is 99.13%.
Embodiment 3
Utilize phosphatization waste residue to produce a method for tricalcium phosphate co-production ferric oxide, comprise the following steps:
(1) phosphatization waste residue pre-treatment: phosphatization waste residue is placed in pulverizer and is ground into 110 object powder, again powder is placed in pretreatment pool, be that 2.5:1 mixes according to powder and the proportioning of oxidizing acid, during mixing, oxidizing acid is added in pretreatment pool, and the stirring velocity that employing stirring speed is 40r/min carries out stir process, after property to be oxidized acid has added, after Keep agitation speed stirs 40min, adjustment temperature is 40 DEG C, leave standstill 30min, add the water of 2.5 times of powder weight more wherein, and to adjust stirring velocity be 110r/min, after Keep agitation 45min, stop stirring, and carried out filtration treatment, obtain filter residue and filtrate, filter residue is transported to Building Materials Factory and produces building materials, filtrate gives over to stand-by,
(2) alkalize: by step 1) filtrate that obtains proceeds in alkalization pond, and limit adds sodium hydroxide limit and takes stirring velocity to be 45r/min stir process wherein, temperature in adjustment alkalization pond is 75 DEG C, when having a large amount of reddish-brown precipitations to occur in extremely alkalization pond to be added, adjustment stirring velocity is 115r/min, and after continuing to add the sodium hydroxide of phosphatization waste residue weight 0.5 times wherein, Keep agitation 15min, stop stir process, and adjust temperature be at 60 DEG C leave standstill, stand-by;
(3) be separated: by step 2) in the solution containing precipitation be placed in separating machine, carry out solid-liquid separation process, obtain solid and liquid, wherein solid is placed in drying machine, after adopting the temperature drying treatment 20s of 95 DEG C, acquisition ferric oxide; Liquid is stand-by;
(4) heat: by step 3) obtain liquid be placed in well heater, heat-up rate is adopted to be 1 DEG C/min hyperthermic treatment, and when hyperthermic treatment, add calcium chloride solution wherein, treat that the pH value of solution reaches 11.3, stop adding of calcium chloride solution, employing stirring speed is after 75r/min stir process 25min, stop hyperthermic treatment, and to adjust temperature is after 65 DEG C, carried out filtration treatment, obtained solid phase and liquid phase; Solid phase is placed in drying machine and adopts the dry 35s of the temperature of 90 DEG C, obtains tricalcium phosphate; Liquid phase is stand-by;
(5) cooling: by step 4) liquid phase that obtains is placed in after water cooler carries out cooling process to 3 DEG C, be placed on again in separating machine and carry out separating treatment, obtain waste liquid and precipitation, calcium chloride dissolution process is carried out in waste back-cycling calcium chloride dissolving tank, precipitation adopts clear water to be after 1:3 mixes according to precipitating with the mass ratio of clear water, employing stirring speed is after 50r/min stir process 15min, and after being warming up to 25 DEG C, be placed on again in separator and carry out filtration treatment, obtain liquid phase A and solid phase A, solid phase A is placed in after calcium chloride dissolving tank dissolves once again, add step 4 again) in, liquid phase A is placed in cooling crystallizer and carries out the process of repetition crystallisation by cooling, repeat crystallisation by cooling process and reduce temperature to-1 DEG C, after leaving standstill cooling process 40min, filtered, obtain waste liquid A and solid A, waste liquid A returns the dissolving carrying out calcium chloride in calcium chloride dissolving tank again, solid A is placed in drying machine, after adopting the dry 40s of the temperature of 75 DEG C, obtain sodium-chlor product, can complete and adopt phosphatization waste residue to produce tricalcium phosphate.
Described sodium hydroxide to be mass percent be 55% solution.
Described oxidizing acid is hypochlorous acid.
Described calcium chloride solution adopts water to dissolve calcium chloride in calcium chloride dissolving tank, and then formulated mass percent is the solution of 60%.
Measure the rate of recovery of ferro element: can learn that the pick-up rate of ferric oxide is 99.24%;
Measure the purity of tricalcium phosphate, can learn, the purity of tricalcium phosphate is 98.15%.
It is important to point out at this; above embodiment is only limitted to understand technical scheme of the present invention and illustrate; it is not the further restriction to technical scheme of the present invention; those skilled in the art make the essential characteristics of non-protruding and the improvement of non-significant progress on this basis, all belong to protection category of the present invention.
Claims (4)
1. utilize phosphatization waste residue to produce a method for tricalcium phosphate co-production ferric oxide, it is characterized in that, comprise the following steps:
(1) phosphatization waste residue pre-treatment: phosphatization waste residue is placed in pulverizer and is ground into 100-120 object powder, again powder is placed in pretreatment pool, be (2-3) according to powder with the proportioning of oxidizing acid: 1 mixes, during mixing, oxidizing acid is added in pretreatment pool, and the stirring velocity that employing stirring speed is 30-50r/min carries out stir process, after property to be oxidized acid has added, after Keep agitation speed stirs 30-50min, adjustment temperature is 30-55 DEG C, leave standstill 20-40min, add the 2-3 water doubly of powder weight more wherein, and to adjust stirring velocity be 100-120r/min, after Keep agitation 30-60min, stop stirring, and carried out filtration treatment, obtain filter residue and filtrate, filter residue is transported to Building Materials Factory and produces building materials, filtrate gives over to stand-by,
(2) alkalize: by step 1) filtrate that obtains proceeds in alkalization pond, and limit adds sodium hydroxide limit and takes stirring velocity to be 40-50r/min stir process wherein, temperature in adjustment alkalization pond is 70-80 DEG C, when having a large amount of reddish-brown precipitations to occur in extremely alkalization pond to be added, adjustment stirring velocity is 100-130r/min, and after continuing to add phosphatization waste residue weight 0.4-0.9 sodium hydroxide doubly wherein, Keep agitation 10-20min, stop stir process, and adjust temperature be at 50-70 DEG C leave standstill, stand-by;
(3) be separated: by step 2) in the solution containing precipitation be placed in separating machine, carry out solid-liquid separation process, obtain solid and liquid, wherein solid is placed in drying machine, after adopting the temperature drying treatment 10-30s of 90-100 DEG C, acquisition ferric oxide; Liquid is stand-by;
(4) heat: by step 3) obtain liquid be placed in well heater, heat-up rate is adopted to be 1 DEG C/min hyperthermic treatment, and when hyperthermic treatment, add calcium chloride solution wherein, treat that the pH value of solution reaches 10-12.1, stop adding of calcium chloride solution, employing stirring speed is after 60-90r/min stir process 20-30min, stop hyperthermic treatment, and to adjust temperature is after 60-70 DEG C, carried out filtration treatment, obtained solid phase and liquid phase; Solid phase is placed in drying machine and adopts the dry 30-40s of the temperature of 90 DEG C, obtains tricalcium phosphate; Liquid phase is stand-by;
(5) cooling: by step 4) liquid phase that obtains is placed in water cooler and carries out cooling process to after 0-5 DEG C, be placed on again in separating machine and carry out separating treatment, obtain waste liquid and precipitation, calcium chloride dissolution process is carried out in waste back-cycling calcium chloride dissolving tank, precipitation adopt clear water according to precipitation and the mass ratio of clear water be 1: 3 mix after, employing stirring speed is after 40-60r/min stir process 10-20min, and after being warming up to 20-30 DEG C, be placed on again in separator and carry out filtration treatment, obtain liquid phase A and solid phase A, solid phase A is placed in after calcium chloride dissolving tank dissolves once again, add step 4 again) in, liquid phase A is placed in cooling crystallizer and carries out the process of repetition crystallisation by cooling, repeat crystallisation by cooling process and reduce temperature to≤3 DEG C, after leaving standstill cooling process 20-50min, filtered, obtain waste liquid A and solid A, waste liquid A returns the dissolving carrying out calcium chloride in calcium chloride dissolving tank again, solid A is placed in drying machine, after adopting the dry 30-50s of the temperature of 70-80 DEG C, obtain sodium-chlor product, can complete and adopt phosphatization waste residue to produce tricalcium phosphate co-production ferric oxide.
2. utilize phosphatization waste residue to produce the method for tricalcium phosphate co-production ferric oxide as claimed in claim 1, it is characterized in that, described sodium hydroxide employing mass percent is that the sodium hydroxide solution of 30-70% replaces.
3. utilize phosphatization waste residue to produce the method for tricalcium phosphate co-production ferric oxide as claimed in claim 1, it is characterized in that, described oxidizing acid is hypochlorous acid.
4. utilize phosphatization waste residue to produce the method for tricalcium phosphate co-production ferric oxide as claimed in claim 1, it is characterized in that, described calcium chloride solution adopts water to dissolve calcium chloride in calcium chloride dissolving tank, and then formulated mass percent is the solution of 50-70%.
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| CN105776165B (en) * | 2016-02-29 | 2018-03-23 | 嘉兴双军环保科技有限公司 | A kind of method for preparing ferric phosphate using phosphatization waste residue extraction |
| CN105772043B (en) * | 2016-03-30 | 2018-07-27 | 上海第二工业大学 | A method of preparing dyestuff Photodegradation catalyst using phosphatization slag |
| CN111017897A (en) * | 2019-12-23 | 2020-04-17 | 泰安市永达环保科技有限公司 | Phosphating waste residue recycling treatment equipment and treatment method |
| CN111690280A (en) * | 2020-07-06 | 2020-09-22 | 湘潭市双马世纪新材料有限公司 | Method for producing phosphate antirust pigment by using phosphated residue |
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| US4986977A (en) * | 1989-12-12 | 1991-01-22 | Man-Gill Chemical Company | Recovery of useful products from by-products of phosphate conversion coating process |
| CN102849701A (en) * | 2012-08-31 | 2013-01-02 | 沈阳理工大学 | Method of extracting phosphorus from chemical nickel-phosphorus plating waste liquid for preparation of calcium phosphate |
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| CN104118853A (en) * | 2014-06-20 | 2014-10-29 | 马鞍山市华清环保工程有限公司 | Metal surface treatment phosphated residue comprehensive utilization method |
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| US4986977A (en) * | 1989-12-12 | 1991-01-22 | Man-Gill Chemical Company | Recovery of useful products from by-products of phosphate conversion coating process |
| CN102849701A (en) * | 2012-08-31 | 2013-01-02 | 沈阳理工大学 | Method of extracting phosphorus from chemical nickel-phosphorus plating waste liquid for preparation of calcium phosphate |
| CN103395761A (en) * | 2013-07-29 | 2013-11-20 | 丁忠华 | Method for preparing phosphate and iron oxide red by utilizing phosphated residue |
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