CN108602673A - The device of Joint Production for phosphate and potassium sulfate - Google Patents
The device of Joint Production for phosphate and potassium sulfate Download PDFInfo
- Publication number
- CN108602673A CN108602673A CN201780009438.8A CN201780009438A CN108602673A CN 108602673 A CN108602673 A CN 108602673A CN 201780009438 A CN201780009438 A CN 201780009438A CN 108602673 A CN108602673 A CN 108602673A
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- Prior art keywords
- phosphate
- hydrochloric acid
- equipment
- component
- producing
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/32—Phosphates of magnesium, calcium, strontium, or barium
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/01—Treating phosphate ores or other raw phosphate materials to obtain phosphorus or phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D1/00—Oxides or hydroxides of sodium, potassium or alkali metals in general
- C01D1/02—Oxides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/02—Preparation of sulfates from alkali metal salts and sulfuric acid or bisulfates; Preparation of bisulfates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05D—INORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C; FERTILISERS PRODUCING CARBON DIOXIDE
- C05D1/00—Fertilisers containing potassium
Abstract
The present invention relates to technical field of chemistry, and more particularly relate to the device of the Joint Production of phosphate such as Dicalcium Phosphate and/or tricalcium phosphate and potassium sulfate, described device includes for the unit by potassium chloride and gas washing in SA production potassium sulfate and hydrochloric acid, it includes the stove for producing potassium sulfate, equipment for producing hydrochloric acid by exhaust gas and the component for being used to prepare the hydrochloric acid for extraction, and for producing phosphatic unit by phosphatic raw materials, it includes equipment of the HCl extract component with the solution for neutralization is used to prepare, it is connected to liquid phase neutralization and calcium phosphate precipitation component by main pipeline, it continuously arranges downstream the following terms connected by conveyance conduit：Phosphate separator-filter, phosphate wash and phosphate drying equipment, the equipment of separation solid phase and liquid phase is set between HCl extract component and liquid phase neutralization and calcium phosphate precipitation component after being wherein used to extract, and it is in connection by main pipeline, and the stove for being used to produce potassium sulfate is connected to via gas vent for the equipment by exhaust gas production hydrochloric acid by pipeline, the latter is connected to HCl extract component by pipeline via the component for being used to prepare the hydrochloric acid for extraction.
Description
Technical field
The present invention relates to technical field of chemistry, and more particularly relate to Joint Production phosphate such as Dicalcium Phosphate and/
Or the device of tricalcium phosphate and potassium sulfate.
Background technology
Modern Fertilizer Market widespread demand phosphate and potassium sulfate.The former is for producing various phosphatic manure products, and sulfuric acid
Potassium itself is chlorideless potassic fertilizer.This is why exploitation for the efficient of its production and has cost in current chemical technology
The equipment of benefit is highly relevant problem.
It has been currently known considerable document and has disclosed and ore is reduced phosphate by using hydrochloric acid and produces phosphate.Example
Such as, the certificate SU1470663 of the present inventor is disclosed produces Dicalcium Phosphate as result below：In 35- in water slurry
At a temperature of 40 DEG C, the hydrochloric acid charging rate of 0.24-0.60kg/h/100g apatite, 35% hydrochloric acid of phosphatic raw materials are used
Decomposition.Document SU842083 and SU994457 are disclosed and are produced compound fertilizer by phosphatic raw materials by the way that its hydrochloric acid is decomposed,
Wherein decompose includes using dilute hydrochloric acid (1-4%).However, source and the use of hydrochloric acid are not all instructed or shown to all files
In the equipment of production process.
Immediate with the present invention is for producing phosphatic device comprising HCl extract component is used to prepare use
In the equipment of the solution of neutralization, liquid phase neutralizes and calcium phosphate precipitation component, phosphate separator-filter, phosphate wash and
Phosphate drying equipment is (referring to Dzhafarov I.Ph.Precipitate production.Moscow, Publishing
House " Food Industry ", 1975, p.5-57).It is used as it is known that being produced by skeleton soil by the method for HCl extract
The device of the Dicalcium Phosphate of feed phosphate.However the form that HCl extract component is reactor (impregnating equipment), it is continuous to combine
And cascade (group) or library is formed by the cocurrent of hydrochloric acid and HCl extract product, and liquid phase neutralize and calcium phosphate precipitation component with
The form of several reactors (settling vessel) being continuously connected with each other is made to ensure the continuity of process, and is equipped with for collecting
With the tank of equalization phosphate slurries preparation, the equipment for being used to prepare the solution for neutralization is to be used to prepare setting for milk of lime
It is standby, therefore, allow the good recycling of the phosphatic raw materials (skeleton soil) of high quality, eliminates and used in leaching stages for dividing
Attachment device from solid phase and liquid phase (semisolid debirs are removed by being sucked by vacuum from reactor).However, due to
The charging stage of rock phosphate in powder, especially low quality ore recycling saves this equipment, solid extraction waste can block neutralization and
The reactor of calcium phosphate precipitation unit, and the then phosphatic reactor of itself blocking products-.This can limit the effect of known devices
Rate and use field.In addition, for operating device, need external hydrochloric acid source, be the hydrochloric acid of input, needed for amount exist
Not always obtainable in technology and logistics, latter of which, which can increase the cost of phosphate production and limit it, uses field.
Invention content
This is why the object of the present invention is to provide a kind of devices of the decomposition for phosphatic raw materials comprising mistake
The unit for producing hydrochloric acid of Cheng Suoxu simultaneously makes it possible to produce phosphate and potassium sulfate simultaneously.
This purpose is realized for the result of Joint Production phosphate and the new equipment of potassium sulfate as exploitation, should
Device includes：
For the unit by potassium chloride and gas washing in SA production potassium sulfate and hydrochloric acid comprising the stove for producing potassium sulfate is used
In the equipment and the component for being used to prepare the hydrochloric acid for extraction that produce hydrochloric acid by exhaust gas, and
For producing phosphatic unit by phosphatic raw materials comprising HCl extract component is used to prepare for neutralizing
Solution equipment, the equipment by main pipeline be connected to liquid phase neutralize and calcium phosphate precipitation component, downstream for pass through conveying
The following terms of pipe connection continuously arranged：Phosphate separator-filter, phosphate wash and phosphoric acid salt drying device,
Equipment wherein for detaching solid phase and liquid phase after extraction is arranged in hydrochloric acid leaching component and liquid phase and and phosphorus
Between hydrochlorate precipitates component, and it is connected thereto by main pipeline, and the stove for being used to produce potassium sulfate is gone out by pipeline via gas
Mouth is connected to the equipment for producing hydrochloric acid by exhaust gas, and the latter is by pipeline via the component for being used to prepare the hydrochloric acid for extraction
It is connected to hydrochloric acid leaching component.
Basic fundamental effect provided by the invention is, can produce phosphate by the phosphatic raw materials of different qualities,
By ensuring for the optimization for giving the best production model and condition of raw material, and valuable mineral are produced on device simultaneously
Fertilizer potassium sulfate.In addition, the apparatus according to the invention allow to significantly reduce raw material transportation cost and optimize the energy at
This.
The apparatus according to the invention is designed for producing following phosphate：Dicalcium Phosphate, tricalcium phosphate and its mixture, with
And Dicalcium Phosphate, tricalcium phosphate with comprising phosphatic minerals, such as the mixture with fluor-apatite.Including more than 20%
The rock phosphate in powder (phosphate rock, apatite) of phosphorus pentoxide is for producing phosphate.The apparatus according to the invention allows to produce
Commercial product (phosphate) is dry phosphorus in HCl extract (the phosphate ores decomposition) for being generated by device itself
Hydrochlorate.In the apparatus of the present, as use gas washing in SA production hydrochloric acid as a result, producing valuable chlorideless potassic fertilizer-sulfuric acid
Potassium.The amount of hydrochloric acid needed for the extraction generated by exhaust gas is directly directly proportional to the volume of the potassium sulfate produced, and the hydrochloric acid
Concentration can be up to 33wt%, and optimum extraction pattern is selected to provide the type for depending on phosphatic raw materials and quality, special
It is not the chance that optium concentration and acid spending rate are selected for most types of phosphatic raw materials.By potassium chloride and gas washing in SA production
The unit of potassium sulfate and hydrochloric acid, include stove for producing potassium sulfate and including in a device setting for hydrochloric acid is produced by exhaust gas
It is standby, contribute to the manufacturing process for implementing potassium sulfate in the device and in the apparatus hydrochloric acid of the production for extraction；And it is filling
Set being used to prepare for middle offer contributes to desired optium concentration of the production with raw material using the component of the hydrochloric acid of extraction
The desired amount of hydrochloric acid.It is used to prepare the equipment of the solution for neutralization and mounted on for producing phosphate by phosphatic raw materials
Unit in liquid phase neutralize and calcium phosphate precipitation component makes it possible to produce and desired in phosphate product determines matter and quantitative
Phosphatic formula, and the equipment for detaching solid phase and liquid phase after extraction.Wherein, separation solid phase and liquid phase after being used to extract
Equipment, phosphate separator-filter, phosphate wash ensures high product purity, and drying equipment complete it is commercially available
Phosphatic production.The device of the invention of complex with the feature is ensured is determined matter and is quantified by raw material with different
Formula produces commercially available phosphate, and ensures the continuity and high efficiency of process simultaneously.
Therefore, different from the solution of the prior art, present invention firstly provides former for the phosphate by different qualities
Material produces commercially available phosphatic device, by the way that optimized operation mode and condition ensure in terms of raw material or final products, uses
The exhaust gas HCl extract phosphatic raw materials generated in the device, and for producing the new product of this device and valuable production
Product-potassium sulfate.Other than the production of hydrochloric acid, equipment of the invention uses sulfuric acid and potassium chloride, is obtainable and cheap
Raw material, to help to realize described device at industrial scale.
Description of the drawings
Fig. 1 is the construction of the apparatus according to the invention and the schematic diagram of operation.
Specific implementation mode
Equipment for producing phosphate and potassium sulfate includes for producing phosphatic unit B comprising has and is used for
The HCl extract component 4 of the entrance of phosphatic raw materials and hydrochloric acid, the equipment 5 for detaching solid phase and liquid phase after leaching, liquid
Mutually neutralization and calcium phosphate precipitation component 6 are used to prepare the equipment 7 using the solution neutralized, phosphate separator-filter 8, phosphoric acid
Salt wash 9, phosphate drying equipment 10, and the device A for producing potassium sulfate and hydrochloric acid, it includes for producing sulphur
The stove 1 of sour potassium, the equipment 2 for producing hydrochloric acid by exhaust gas and the component 3 for being used to prepare the hydrochloric acid using extraction.Wherein, hydrochloric acid
The outlet of extraction component 4 is connected to the entrance of the equipment 5 for detaching solid phase and liquid phase after extraction by pipeline, for solid phase
The outlet of equipment 5 is to be exported for the device of solid waste, and it is used to the outlet of liquid phase and is connected to by pipeline be used for
The entrance of the extraction liquid phase of liquid phase neutralization and calcium phosphate precipitation unit 6 is fed, liquid phase neutralizes and the use of the unit 6 of calcium phosphate precipitation
The outlet for being used to prepare the equipment 7 using the solution neutralized is connected to by pipeline in the entrance of the solution of neutralization, liquid phase neutralizes
And the outlet of calcium phosphate precipitation component 6 is connected to the entrance of phosphate separator-filter 8 by pipeline, it is device to be used to export
The outlet for liquid wastes, and its be used for it is phosphatic outlet by transport pipeline via phosphate wash 9 connect
To phosphate drying equipment 10, the outlet of equipment 10 is the outlet for commercial product of device, the stove 1 for producing potassium sulfate
With for potassium chloride and sulfuric acid entrance and for the outlet of product, and the outlet for gas of stove 1 is connected by pipeline
To the entrance of the equipment 2 for producing hydrochloric acid by exhaust gas, the equipment 2 for producing hydrochloric acid by exhaust gas also has entering for water supply
Mouthful, and its outlet is connected to the entrance for the component 3 for being used to prepare the hydrochloric acid for extraction by pipeline, second entrance is that water enters
Mouthful, and be used to prepare hydrochloric acid for extraction component 3 outlet by pipeline be connected to HCl extract component 4 for hydrochloric acid
Entrance.
Device is run as follows.The desired amount of potassium chloride and the concentrated sulfuric acid are fed into stove 1, wherein the knot as pyroreaction
Fruit generates potassium sulfate, and the hot gas containing gaseous hydrogen chloride is removed via conveyance conduit from stove, into for by exhaust gas
In the equipment 2 for producing hydrochloric acid.In equipment 2, gas is cooled, and hydrogen chloride is fed to the water in equipment 2 and absorbs and with hydrochloric acid
Form accumulate in equipment 2.When exhaust gas concentration of hydrochloric acid is higher, acid is pumped into via pipeline and is used to prepare for extraction
The component 3 of hydrochloric acid.In component 3, hydrochloric acid is obtained to scheduled concentration, and the hydrochloric acid with predetermined concentration is grasped with factory
Amount accumulation needed for making.Meanwhile in the equipment 7 for being used to prepare the solution of sum used in, neutralizer being mixed with water and is obtained
The solution (milk of lime, calcium carbonate suspension etc.) for neutralization with predetermined concentration.
By the desired amount of phosphatic raw materials with required dispersion degree, such as salt is fed in the form of the phosphate rock ground
In acidleach bill of lading member 4, wherein hydrochloric acid is fed by component 3 in wherein with required concentration and required amount simultaneously.In component 4
In, under the action of hydrochloric acid, phosphate transfection moves on in solution, and is formed mainly comprising one-lime phosphate, soluble gold in exit
Belong to the slurries of chloride and solid impurity.The slurries quilt of the equipment 5 for detaching solid phase and liquid phase after extraction is transferred to from component 4
Being separated into the form of solid waste can be by the liquid phase for the solid phase and acid solution form that device removes, and wherein liquid phase includes mainly phosphoric acid
One calcium and soluble impurity.Into neutralize and calcium phosphate precipitation sub-assembly 6 phosphate and soluble impurity acid solution with from
It is used to prepare the equipment 7 of the solution for neutralization to mix with the solution for neutralization that required amount is transmitted, when mixture pH increases
One-lime phosphate is transformed into the Dicalcium Phosphate that can be precipitated and (and even transforms into tricresyl phosphate with selected appropriate mode when adding to desirable value
Calcium or phosphate mixt).The phosphate slurries generated in unit 6 enter phosphate separator-filter 8.It is mainly chlorination to collect
Calcium, magnesium chloride or other dirt solution forms the filtrate from filter 8 and removed from device in the form of liquid debris,
And guide the solid residue of Dicalcium Phosphate (or another corresponding phosphate) to phosphate wash 9, wherein
It washes and filtering or according to mutually detaching (wash liquid of pollution as liquid wastes discharge) again again, and with rear feeding to phosphoric acid
Salt drying equipment 10 obtains finished product phosphate in its exit.In corresponding device (not shown), absorb and purification of salts acidleach
The gas generated in bill of lading member 4 and neutralization and calcium phosphate precipitation unit 6.
When the formula of the phosphatic raw materials used changes, in the component 3 for being used to prepare the hydrochloric acid for extraction, it is based on
The exhaust gas hydrochloric acid of concentration prepares the optium concentration of the exhaust gas hydrochloric acid for given raw material, with the amount and quality with raw material at
The required amount of ratio is transferred in extraction component 4, and in the device 7 for being used to prepare the solution of sum used in, needed for preparation
Thus the solution for neutralization of concentration and amount provides optimum condition and pattern for phosphate production.
The solid waste generated in the equipment 5 for detaching solid phase and liquid phase after for extraction is abandoned.From phosphoric acid salinity
Liquid wastes from filter 8 and wash 9 pour into it is marine, alternatively, if it is not possible, by known method,
It is recycled into solid waste or commercial product for example, by evaporation.
A part of the potassium sulfate generated in stove 8 as valuable fertilizer individually or as mixing or compound fertilizer goes out
It sells.
Unit, equipment and the component of device are implemented in known manner.For example, HCl extract component 4 and liquid phase neutralize and
Calcium phosphate precipitation component 6 can be made for one or more reactors continuously arranged, and (hereinafter " reactor " is that have stirring
The tank of device has the nozzle for liquid phase input and slurries output, supplies the phosphatic raw materials of heat partition or for the molten of neutralization
The nozzle of liquid or port (there is disk and conveyance conduit)), reactor can combine and form cascade or library, and by cocurrent with
Raw material or the corresponding solution for neutralization are combined to the supply in one or more reactors of the cascade (library) of component 4 or 6.
Component 4,6 can be made based on Multi sectional reactor (extraction unit).Under these conditions, the primary condition of device continuous operation
It is that there is the tank of blender or the accumulation tank of blender does not exist in component 4,6 in accumulation reactor, wherein extraction slurry
Liquid or phosphate slurries preparation are collected and are homogenized before a distribution between equipment 5 and filter 8 respectively.It is reacted as accumulation
Device can use the last one section of the last one cascade reactor or Multi sectional reactor.By phosphatic raw materials or
In the case of in the solution feed to multiple reactors (determination) of neutralization, component 4,6 can be respectively included for existing respectively
The equipment that phosphatic raw materials or the solution for neutralization are distributed between reactor, tool can for example be made, and there are one entrances and more
A outlet that reactor is connected to by pipeline, and control the form with the tank (reactor) of measuring apparatus.
The shape of mixer (reactor with blender) can be made for by being used to prepare the equipment 7 of the solution for neutralization
Formula, the wherein setting value of dispensing solid neutralizer and water.
Multiple accumulation tanks can be made for by being used to prepare the component 3 of the hydrochloric acid for extraction, the tank (reaction with mixer
Device) form, equipped with the pumping, control and measuring apparatus connected by pipeline.
Equipment 5 for detaching solid phase and liquid phase after extraction can be made for typical separator, and (separator, filtering are set
It is standby) form, for example, the form of filter press.
Phosphate separator-filter 8 is also conventionally produced as the form of the form of different type filter plant, such as filter press,
Some includes wash (rotation and band filter).For example, when using band filter as filter 8, phosphoric acid
Salt passes through supply to the water washing on a part of belt filter.In order to filter and wash phosphate, drum-type vacuum can be used
Filter etc..
Phosphate wash 9 and phosphate drying equipment 10 are also implemented in known manner.For example, with blender and
The tank of settler may be used as individual wash.In addition, also fluid bed dryer, drum-type, canal drier and
Other washings generated conventionally used for precipitation and drying device.
As stove 1, the Muffle furnace with waste gas burning heating and other kinds of stove can be used.For being given birth to by exhaust gas
The equipment 2 of production hydrochloric acid can be implemented in the form of heat insulation-type gas cooler, such as a series of absorption towers being connected with each other successively
The absorber of form, such as exhaust gas hydrochloric acid collector-accumulator.
It measures using typical control with dispensing liquid and dispersing liquid and slurry, device in order to pump and pumping is set
It is standby, and for feed solids raw material, remove product and waste material, conveyance conduit, Pneumatic pipe and other types can be used
Equipment.
In view of the above, the apparatus according to the invention can be made and use on an industrial scale.
The present invention will be explained in further detail in the following embodiments, however, these embodiments should not be regarded as to power
The limitation for the range that profit requires.
Embodiment：
Embodiment 1
Dry potassium chloride is fed to the stove with heating ceiling of the unit A for producing hydrochloric acid with the rate of 51kg/h
In 1, and a concentration of 98% sulfuric acid is entered with the rate dispensing of 35kg/h in reaction zone.Process is run at a temperature of 400 DEG C,
The potassium sulfate of chlorideless potassic fertilizer is wherein produced with the rate of 62kg/h.The chlorination hydrogen migration discharged in gaseous form is inhaled for water
It receives, wherein generating in three continuous absorption towers 31% hydrochloric acid with the rate of 78kg/h.Be diluted with water to 12% it is dense
When spending, hydrochloric acid is transferred to the rate of 200kg/h for being produced in phosphatic unit B by phosphatic raw materials.
The phosphatic raw materials of crushing phos-phate forms with the parts 1-2mm are fed to the reactor grade with blender
In the HCl extract component 4 of connection.The phosphate of crushing is fed to the first reactor of reactor cascade with the rate of 44kg/h
In be used for ore decomposition.In an identical manner, 12% hydrochloric acid is fed with the rate of 200kg/h.Process is in 60 DEG C of temperature and big
It is run under air pressure.By the slurry comprising in terms of phosphorus pentoxide 4.9% phosphate and 4.2% insoluble residue from system
It is fed in filtration step.During filtering, insoluble residue is isolated, and phosphate solution is fed to neutralization and phosphoric acid
Salt precipitates in component 6, is the reactor cascade with blender.At 60 DEG C of temperature and atmospheric pressure, as with 30kg/h
Rate introduces into cascade reactor the knot of 33% calcium carbonate water slurries from the equipment 7 for being used to prepare the solution for neutralization
Fruit, reaction mass are partially neutralized.Meanwhile the pH levels in reaction zone are increased to 3.5, and phosphate transfection is caused to become not soluble in water
Form.It will be transferred in filtration step from reactor comprising in terms of phosphorus pentoxide 4.1% phosphatic slurries, wherein solid
Body phosphate is detached and is transferred to water-washing step in the form of wet cake under the rate of the 26kg/h in terms of siccative, until chlorion contains
Amount is no more than 0.1%, and then to drying steps and to obtain 5% moisture content.18% will isolated in filter process
Calcium chloride solution transfer is abandoned.
Claims (6)
1. a kind of device for Joint Production phosphate and potassium sulfate, including：
Include for producing the stove of potassium sulfate, for by giving up for the unit by potassium chloride and gas washing in SA production potassium sulfate and hydrochloric acid
The equipment of gas production hydrochloric acid and the component for being used to prepare the hydrochloric acid for extraction, and
For producing phosphatic unit, including HCl extract component by phosphatic raw materials, it is used to prepare the solution for neutralization
Equipment, the equipment is connected to that liquid phase neutralizes and calcium phosphate precipitation component, downstream continuous arrangement pass through defeated by main pipeline
The following terms for sending pipeline to connect：Phosphate separator-filter, phosphate wash and phosphate drying equipment,
The equipment for being wherein used to detach solid phase and liquid phase after extraction be set in the HCl extract component and the liquid phase and
And between calcium phosphate precipitation component, and it is in connection by main pipeline, and the stove for producing potassium sulfate passes through pipe
Road is connected to the equipment for producing hydrochloric acid by exhaust gas via gas vent, and the latter is used to prepare by pipeline via described
The component of hydrochloric acid for extraction is connected to the HCl extract component.
2. the apparatus according to claim 1, which is characterized in that as phosphate obtain Dicalcium Phosphate, tricalcium phosphate and it
Mixture and Dicalcium Phosphate and/or tricalcium phosphate and the mixture comprising phosphatic mineral, particularly fluor-apatite.
3. the apparatus according to claim 1, which is characterized in that produced in the device for producing hydrochloric acid by exhaust gas
Concentrated hydrochloric acid.
4. device according to claim 3, which is characterized in that produced in the device for producing hydrochloric acid by exhaust gas
Hydrochloric acid has the concentration less than or equal to 33wt.%.
5. the apparatus according to claim 1, which is characterized in that phosphatic using being used for more than 20% phosphorus pentoxide
Production.
6. the apparatus according to claim 1, which is characterized in that for HCl extract and liquid phase neutralizes and calcium phosphate precipitation
Component implemented in the form of the reactors continuously arranged of one or more, the reactor can combine and formed cascade or
Library, and combined by cocurrent, wherein raw material or the corresponding solution for neutralization are supplied to the first of the cascade or library
In a or multiple reactors.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| RU2016112592 | 2016-04-04 | ||
| RU2016112592A RU2616061C1 (en) | 2016-04-04 | 2016-04-04 | Installation for combined obtaining of phosphate salts and potassium sulphate |
| PCT/RU2017/000191 WO2017176164A1 (en) | 2016-04-04 | 2017-03-31 | Plant for the combined production of phosphate salts and potassium sulphate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108602673A true CN108602673A (en) | 2018-09-28 |
| CN108602673B CN108602673B (en) | 2022-12-09 |
Family
ID=58642911
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780009438.8A Active CN108602673B (en) | 2016-04-04 | 2017-03-31 | Device for the joint production of phosphate and potassium sulphate |
Country Status (4)
| Country | Link |
|---|---|
| CN (1) | CN108602673B (en) |
| EA (1) | EA030179B1 (en) |
| RU (1) | RU2616061C1 (en) |
| WO (1) | WO2017176164A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111232940B (en) * | 2020-03-12 | 2023-05-02 | 连云港树人科创食品添加剂有限公司 | Preparation method of tricalcium phosphate and potassium chloride in co-production |
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| CN1152549A (en) * | 1996-11-21 | 1997-06-25 | 戴文清 | Technology for preparing potassium sulfate by two-stage method |
| CN1962421A (en) * | 2006-11-19 | 2007-05-16 | 武善东 | Phosphorite acidolysis method |
| CN101337657A (en) * | 2008-08-06 | 2009-01-07 | 黄明科 | Process for disassembling phosphate ore by mixed acid and coproducing potassium dihydrogen phosphate, hydrogen phosphate and combined fertilizer |
| CN102417169A (en) * | 2011-08-15 | 2012-04-18 | 武善东 | Acidolysis method of magnesium-containing phosphate rock |
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| US2706145A (en) * | 1950-02-28 | 1955-04-12 | Curtis W Cannon | Production of sulphates and hci |
| US3803884A (en) * | 1969-01-09 | 1974-04-16 | Fitzwilton Ltd | Production of fertilizers |
| US3919395A (en) * | 1970-11-18 | 1975-11-11 | United States Gypsum Co | Process for extraction of phosphorus compounds |
| US4045543A (en) * | 1975-11-12 | 1977-08-30 | Pennzoil Company | Production of potassium sulfate and hydrogen chloride |
| US4328196A (en) * | 1980-09-25 | 1982-05-04 | Pennzoil Company | Production of alkali metal products from alkali metal fluosilicate |
| FI107330B (en) * | 1999-12-03 | 2001-07-13 | Kemira Agro Oy | Preparation of two alkali metal salts by a combined ion exchange and crystallization process |
| BE1015840A3 (en) * | 2003-12-24 | 2005-10-04 | Ecophos | Process leading ore phosphate. |
| CN101066771A (en) * | 2007-05-31 | 2007-11-07 | 聊城大学 | Microwave radiation process for producing potassium sulfate |
| EP2435364B1 (en) * | 2009-05-27 | 2015-05-06 | Easymining Sweden AB | Production of ammonium phosphates |
| CN203922756U (en) * | 2014-06-13 | 2014-11-05 | 江苏瑞和化肥有限公司 | A kind of reactive tank exhaust heat-energy recycling system |
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2016
- 2016-04-04 RU RU2016112592A patent/RU2616061C1/en active
- 2016-12-26 EA EA201692447A patent/EA030179B1/en unknown
-
2017
- 2017-03-31 WO PCT/RU2017/000191 patent/WO2017176164A1/en active Application Filing
- 2017-03-31 CN CN201780009438.8A patent/CN108602673B/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4435370A (en) * | 1981-09-29 | 1984-03-06 | Pennzoil Company | Preparation of monocalcium phosphate and/or phosphoric acid from phosphate rock |
| CN1152549A (en) * | 1996-11-21 | 1997-06-25 | 戴文清 | Technology for preparing potassium sulfate by two-stage method |
| CN1962421A (en) * | 2006-11-19 | 2007-05-16 | 武善东 | Phosphorite acidolysis method |
| CN101337657A (en) * | 2008-08-06 | 2009-01-07 | 黄明科 | Process for disassembling phosphate ore by mixed acid and coproducing potassium dihydrogen phosphate, hydrogen phosphate and combined fertilizer |
| CN102417169A (en) * | 2011-08-15 | 2012-04-18 | 武善东 | Acidolysis method of magnesium-containing phosphate rock |
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| Publication number | Publication date |
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| WO2017176164A1 (en) | 2017-10-12 |
| EA201692447A1 (en) | 2017-10-31 |
| CN108602673B (en) | 2022-12-09 |
| EA030179B1 (en) | 2018-06-29 |
| RU2616061C1 (en) | 2017-04-12 |
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