CN217795002U

CN217795002U - A filter enrichment facility for coprecipitation reaction system

Info

Publication number: CN217795002U
Application number: CN202221345857.3U
Authority: CN
Inventors: 何志; 赵聪; 杨光耀; 何劲松; 康彬
Original assignee: Sichuan Sidaneng Environmental Protection Technology Co ltd; Chengdu Stareng Environmental Protection Equipment Co ltd
Current assignee: Sichuan Sidaneng Environmental Protection Technology Co ltd; Chengdu Stareng Environmental Protection Equipment Co ltd
Priority date: 2022-05-31
Filing date: 2022-05-31
Publication date: 2022-11-15
Anticipated expiration: 2032-05-31

Abstract

The utility model discloses a filter concentration device for coprecipitation reaction system to solve the great technical problem who influences the reaction of filter concentrator volume. A coprecipitation reaction system in which, in a filter concentrator, if a plane perpendicular to the central axis and intersecting a filter surface of the filter element is taken as a cross section: on the cross section, the stock solution cavities are distributed in the form of a first graph, the first graph is a closed graph, the shape of the closed graph is circular, annular or polygonal, the area, except the first graph, of the cross section, which is positioned in the shell of the filtering concentrator, is basically composed of a second graph and a third graph, the clear solution cavities are distributed in the form of the second graph, the filtering materials of the filter element are distributed in the form of the third graph, and the corresponding central points of the central axis on the cross section are close to or positioned in the first graph, the second graph or the third graph.

Description

A filter enrichment facility for coprecipitation reaction system

Technical Field

The embodiments of the present application relate to a co-precipitation reaction system. The coprecipitation reaction system is suitable for preparing the precursor of the anode material of the lithium ion secondary battery, and is particularly suitable for preparing the ternary precursor.

Background

The chemical coprecipitation method is widely applied to liquid-phase chemical synthesis of powder materials, and generally, a proper precipitator is added into a raw material solution, so that all components which are uniformly mixed in the solution are precipitated together according to a stoichiometric ratio, or an intermediate product is precipitated in the solution through reaction, and then is calcined and decomposed to prepare a target product. The process can regulate and control the granularity and the morphology of the product according to experimental conditions, and the effective components in the product can be uniformly mixed at the atomic and molecular level.

At present, the preparation of the ternary precursor of the lithium ion secondary battery anode material is an important application of a chemical coprecipitation method in new energy industry. In the preparation process, nickel sulfate (or nickel chloride), cobalt sulfate (or cobalt chloride) and manganese sulfate (or manganese chloride) are prepared into a mixed salt solution with a certain molar concentration, sodium hydroxide is prepared into an alkali solution with a certain molar concentration, ammonia water with a certain concentration is used as a complexing agent, the mixed salt solution, the alkali solution and the complexing agent are added into a reaction kettle at a certain flow rate, the stirring speed of the reaction kettle, the temperature and the pH value of reaction slurry, the reaction atmosphere (currently, the reaction process is generally required to be completed under the protection of nitrogen) and the like are controlled, so that salt and alkali are subjected to neutralization reaction to generate a ternary precursor crystal nucleus and grow gradually, and after the granularity reaches a preset value, a reaction product is filtered, washed and dried to obtain a ternary precursor. Therefore, the reaction process has more technological parameters to be controlled, and mainly comprises the following steps: salt-to-salt concentration, ammonia water concentration, rate of adding salt solution and alkali solution into the reaction kettle, reaction temperature, pH value during reaction, stirring rate, reaction time, solid content of reaction slurry, reaction atmosphere and the like. And after the preparation of the ternary precursor is finished, uniformly mixing the ternary precursor and a lithium source according to a certain proportion, then calcining, and crushing, grading and drying the cooled material to obtain the lithium ion secondary battery anode material.

For the convenience of production, a filtration concentrator is also arranged beside the reaction kettle at present to implement the concentration outside the kettle. In the operation process of the reaction kettle, reaction raw materials (salt solution, alkali solution and ammonia water) are added into the reaction kettle, part of reaction slurry in the reaction kettle enters a filtering concentrator, a filter element is installed in the filtering concentrator and is provided with a stirring structure, clear liquid can be output from the filtering concentrator after the reaction slurry is filtered by the filter element, the clear liquid can be reused for reaction as mother liquid, and concentrated liquid in the filtering concentrator returns to the reaction kettle through a concentrated slurry backflow structure. The stirring structure in the filtration concentrator is generally including being arranged in the main shaft in the filtration concentrator and installing the epaxial stirring rake in the stirring, and the main shaft is driven by the outside motor of filtration concentrator, and filter core interval arrangement can stir thick liquids when the stirring rake is rotatory, prevents that the particulate matter in the thick liquids from subsiding and prolong filter cake formation time on the filter core. However, the internal structure design of the filtering concentrator leads to larger volume of the filtering concentrator, so that the reaction slurry stays in the filtering concentrator outside the reaction kettle for a longer time, the reaction process is influenced by various process parameters, and once the environment changes, the reaction is influenced, so that the consistency of the reaction and the granularity of the ternary precursor is influenced when the slurry stays in the filtering concentrator for a longer time.

Aiming at the problems brought by the independent arrangement of the filtering concentrator, one solution is to cancel the filtering concentrator and directly install the filter element in a reaction kettle, and at this time, the reaction kettle can be called as co-precipitation reaction and filtering concentration integrated equipment. Because the reaction and the filtration concentration are carried out in the coprecipitation reaction and filtration concentration integrated equipment, the reaction slurry is always in the same environment, and the influence of the independent arrangement of the filtration concentrator on the reaction is avoided. However, it is noted that: the coprecipitation reaction and filtration concentration integrated equipment has higher requirement on the material damage prevention stability of the filter element. If the filter element is damaged, the reaction slurry is contaminated by the material falling off from the filter element.

On the other hand, no matter a coprecipitation reaction system with a separately deployed filter concentrator or a coprecipitation reaction system with a coprecipitation reaction and filter concentration integrated device is adopted, clear liquid filtered by the filter element needs to be output through a clear liquid outlet system. At present, a cleaning system mainly comprises a plurality of parts such as pipelines, valves, backflushing devices and the like, the parts are temporarily installed on site along with the field installation of a filter concentrator or a coprecipitation reaction and filter concentration integrated device, the construction strength is high, the time is long, and the project construction progress is influenced.

SUMMERY OF THE UTILITY MODEL

The embodiment of the application provides a coprecipitation reaction system and a filtering and concentrating device for the same to solve the technical problem that the reaction is influenced by the fact that the volume of a filtering and concentrating device is large.

According to an aspect of the present application, there is provided a coprecipitation reaction system including: the device comprises a coprecipitation reaction unit, a stirring unit and a control unit, wherein the coprecipitation reaction unit comprises a reaction kettle, the reaction kettle is provided with a shell and an inner cavity, a raw material feeding structure, a slurry discharging structure to be concentrated and a concentrated slurry backflow structure are respectively arranged on the shell of the reaction kettle, the raw material feeding structure, the slurry discharging structure to be concentrated and the concentrated slurry backflow structure are respectively communicated with the inner cavity of the reaction kettle, and a stirring structure is arranged in the inner cavity of the reaction kettle; the filtering and concentrating unit comprises a filtering concentrator, the filtering concentrator is provided with a shell and a filter element, the filter element forms a stock solution cavity and a clear solution cavity in the shell of the filtering concentrator, a slurry to be concentrated feeding structure, a concentrated slurry discharging structure and a clear solution discharging structure are respectively arranged on the shell of the filtering concentrator, the slurry to be concentrated feeding structure and the concentrated slurry discharging structure are respectively communicated with the stock solution cavity, and the clear solution discharging structure is communicated with the clear solution cavity; the slurry discharging structure to be concentrated is used for being connected with the slurry feeding structure to be concentrated, the concentrated slurry discharging structure is used for being connected with the concentrated slurry backflow structure, the raw material feeding structure is used for being connected with co-precipitation reaction raw material supply equipment, and the clear liquid discharging structure is used for being connected with a clear liquid discharging system; in the filtering concentrator, the filter element is provided with a first edge and a second edge which are perpendicular to each other, the area of a filtering surface of the filter element is basically determined by the product of the length of the first edge and the length of the second edge, the direction of the length of the first edge is consistent with the direction of a central axis of a shell of the filtering concentrator, and the slurry feeding structure to be concentrated and the concentrated slurry discharging structure are respectively arranged on the shell of the filtering concentrator at positions at two ends of the central axis and are respectively communicated with two ends of a stock solution cavity; if a plane which is perpendicular to the central axis and intersects with the filtering surface of the filter element is taken as a cross section, then: on the cross section, the stock solution cavities are distributed in the form of a first graph, the first graph is a closed graph, the shape of the closed graph is circular, annular or polygonal, the area, except the first graph, of the cross section, which is positioned in the shell of the filtering concentrator, is basically composed of a second graph and a third graph, the clear solution cavities are distributed in the form of the second graph, the filtering materials of the filter element are distributed in the form of the third graph, and the corresponding central points of the central axis on the cross section are close to or positioned in the first graph, the second graph or the third graph.

In the embodiment of the application, the filtering and concentrating unit comprises N filtering and concentrating device components, wherein N is an integer larger than or equal to 1, the filtering and concentrating device components are formed by connecting a plurality of filtering and concentrating devices, and the filtering and concentrating devices are tubular filtering and concentrating devices; the tubular filtering concentrator is provided with a tubular shell and a filter element, the shape and the size of the filter element are matched with those of a pipeline in the shell, an axial channel is arranged in the filter element, and the axial channel forms the stock solution cavity or the clear solution cavity; when the axial channel forms the stock solution cavity, the clear solution cavity is formed between the pipeline in the shell and the filter element, and when the axial channel forms the clear solution cavity, the stock solution cavity is formed between the pipeline in the shell and the filter element; thereby treating concentrated thick liquids feeding structure and concentrated thick liquids ejection of compact structure of tubular filtration concentrator among the filtration concentrator subassembly end to end connection in proper order makes these tubular filtration concentrator's stoste chamber establish ties and be a flow path, the thick liquids feeding structure of treating to concentrate in the flow path first with treat concentrated thick liquids ejection of compact structural connection, the concentrated thick liquids ejection of compact structure of end with concentrated thick liquids backward flow structural connection.

In an embodiment of the present application, the wall of the shell of the tubular filtration concentrator is provided with the clear liquid discharging structure.

In the embodiment of this application, the parallel interval arrangement of tubular filtration concentrator in the filtration concentrator subassembly sets up, thereby the thick liquids feed structure of treating between the adjacent tubular filtration concentrator is connected through the elbow with concentrated thick liquids ejection of compact structure and is made the stoste chamber between the adjacent tubular filtration concentrator establish ties.

In embodiments of the present application, the bends in the filter concentrator assembly are horizontally disposed.

In an embodiment of the present application, the filtration and concentration unit includes more than 2 filtration and concentration device components, and the more than 2 filtration and concentration device components are arranged up and down.

In the embodiment of the application, the clear liquid discharging structures of different tubular filtering concentrators in the same filtering concentrator assembly are converged together to form a group of clear liquid discharging structures, or the clear liquid discharging structures of different tubular filtering concentrators in different filtering concentrator assemblies are converged together to form a group of clear liquid discharging structures; the clear liquid discharging structure corresponds to a group of filter elements, and the clear liquid discharging system performs back flushing regeneration on the filter elements of the same group according to the groups of the filter elements.

In the embodiment of the application, the clear liquid outlet system comprises a clear liquid conveying and filter element backwashing pipeline system, the clear liquid conveying and filter element backwashing pipeline system comprises a clear liquid conveying pipe in one-to-one correspondence with the group of the filter element and a backwashing medium conveying pipe in one-to-one correspondence with the group of the filter element, the output end of the clear liquid conveying pipe is connected with a clear liquid conveying main pipe through a control valve which is arranged in one-to-one correspondence, the input end of the clear liquid conveying pipe is connected with a clear liquid input interface which is used for being connected with a clear liquid discharging structure of the group of the corresponding filter element, the input end of the backwashing medium conveying pipe is connected with a backwashing medium conveying main pipe through a control valve which is arranged in one-to-one correspondence, and the output end of the backwashing medium conveying pipe is connected with a bypass of the clear liquid conveying pipe in one-to-one correspondence; the discharging system further comprises a backflushing device, a backflushing medium input structure and a backflushing medium output structure are arranged on a shell of the backflushing device respectively, and the backflushing medium output structure is connected with the backflushing medium conveying main pipe.

In the embodiment of this application, when the clear liquid ejection of compact structure of different tubular filtration concentrators in the different filtration concentrator subassemblies converges together and forms a set of clear liquid ejection of compact structure, each filtration concentrator subassembly with treat and all be equipped with flow control device between the concentrated thick liquids ejection of compact structure to, all be equipped with back pressure control device on each clear liquid conveyer pipe between the control valve that is located this clear liquid conveyer pipe and the clear liquid conveying main pipe.

In the embodiment of this application, the recoil medium input structure of recoil ware contains recoil liquid input structure and compressed gas input structure, just still be equipped with the recoil liquid overflow mouth on the shell of recoil ware, the recoil liquid overflow mouth is connected to through the recoil liquid overflow pipe the delivery outlet of clear liquid conveying main pipe, then the delivery outlet of clear liquid conveying main pipe is whole to be higher than the recoil liquid overflow mouth, just be equipped with the ascending section on the recoil liquid overflow pipe.

In the embodiment of this application, including vapour and liquid separator, be equipped with vapour and liquid mixed phase input structure on vapour and liquid separator's the shell respectively, by separation liquid phase output structure and by separation gaseous phase output structure, vapour and liquid mixed phase input structure with concentrated thick liquids ejection of compact structural connection, by separation liquid phase output structure with concentrated thick liquids backflow structure connects.

In the embodiment of the application, the device comprises a return pipe, wherein one end of the return pipe is connected with the slurry feeding structure to be concentrated, and the other end of the return pipe is connected with the concentrated slurry discharging structure; the return pipe is at least provided with a valve and a valve in the heat exchange cooler.

In the embodiment of the application, a feeding pump is arranged between the coprecipitation reaction unit and the filtration concentration unit.

According to another aspect of the application, a filtering concentration device for a coprecipitation reaction system is provided, wherein the coprecipitation reaction unit comprises a reaction kettle, the reaction kettle is provided with a shell and an inner cavity, a raw material feeding structure, a slurry discharging structure to be concentrated and a concentrated slurry backflow structure are respectively arranged on the shell of the reaction kettle, the raw material feeding structure, the slurry discharging structure to be concentrated and the concentrated slurry backflow structure are respectively communicated with the inner cavity of the reaction kettle, and a stirring structure is arranged in the inner cavity of the reaction kettle; it includes: the filtering and concentrating unit comprises a filtering concentrator, the filtering concentrator is provided with a shell and a filter element, the filter element forms a stock solution cavity and a clear solution cavity in the shell of the filtering concentrator, a slurry to be concentrated feeding structure, a concentrated slurry discharging structure and a clear solution discharging structure are respectively arranged on the shell of the filtering concentrator, the slurry to be concentrated feeding structure and the concentrated slurry discharging structure are respectively communicated with the stock solution cavity, and the clear solution discharging structure is communicated with the clear solution cavity; the slurry feeding structure to be concentrated is used for being connected with the slurry discharging structure to be concentrated, the concentrated slurry discharging structure is used for being connected with the concentrated slurry backflow structure, and the clear liquid discharging structure is used for being connected with a clear liquid discharging system; in the filtration concentrator, the filter element has a first edge and a second edge which are perpendicular to each other, the area of a filtering surface of the filter element is basically determined by the product of the length of the first edge and the length of the second edge, the direction of the length of the first edge is consistent with the direction of a central axis of a shell of the filtration concentrator, and the slurry feeding structure to be concentrated and the concentrated slurry discharging structure are respectively arranged on the shell of the filtration concentrator at positions at two ends of the central axis and are respectively communicated with two ends of a stock solution cavity; if a plane which is perpendicular to the central axis and intersects the filtering surface of the filter element is taken as a cross section, then: on the cross section, the stock solution cavities are distributed in the form of a first graph, the first graph is a closed graph, the shape of the closed graph is circular, annular or polygonal, the area, except the first graph, of the cross section, which is positioned in the shell of the filter concentrator, is basically composed of a second graph and a third graph, the clear solution cavities are distributed in the form of the second graph, the filter material of the filter element is distributed in the form of the third graph, and the corresponding central point of the central axis on the cross section is close to or positioned in the first graph, the second graph or the third graph.

In an embodiment of the application, the filtration and concentration unit comprises N filtration and concentration assemblies, wherein N is an integer greater than or equal to 1, each filtration and concentration assembly is formed by connecting a plurality of filtration and concentration devices, and each filtration and concentration device is a tubular filtration and concentration device; the tubular filtering concentrator is provided with a tubular shell and a filter element, the shape and the size of the filter element are matched with those of a pipeline in the shell, an axial channel is arranged in the filter element, and the axial channel forms the stock solution cavity or the clear solution cavity; when the axial channel forms the stock solution cavity, the clear solution cavity is formed between the pipeline in the shell and the filter element, and when the axial channel forms the clear solution cavity, the stock solution cavity is formed between the pipeline in the shell and the filter element; thereby treating concentrated thick liquids feeding structure and concentrated thick liquids ejection of compact structure of tubular filtration concentrator among the filtration concentrator subassembly end to end connection in proper order makes these tubular filtration concentrator's stoste chamber establish ties and be a flow path, the thick liquids feeding structure of treating to concentrate in the flow path first with treat concentrated thick liquids ejection of compact structural connection, the concentrated thick liquids ejection of compact structure of end with concentrated thick liquids backward flow structural connection.

In an embodiment of the present application, the wall of the shell of the tube filtration concentrator is provided with the clear liquid discharging structure.

In the embodiment of the application, the clear liquid discharging system comprises a clear liquid conveying and filter element backwashing pipeline system, the clear liquid conveying and filter element backwashing pipeline system comprises clear liquid conveying pipes in one-to-one correspondence with the groups of the filter elements and backwashing medium conveying pipes in one-to-one correspondence with the groups of the filter elements, the output ends of the clear liquid conveying pipes are connected with a clear liquid conveying main pipe through control valves arranged one to one, the input ends of the clear liquid conveying pipes are connected with clear liquid input interfaces used for being connected with clear liquid discharging structures corresponding to the groups of the filter elements, the input ends of the backwashing medium conveying pipes are connected with a backwashing medium conveying main pipe through control valves arranged one to one, and the output ends of the backwashing medium conveying pipes are connected with bypasses of the clear liquid conveying pipes in one-to-one correspondence; the discharging system further comprises a backflushing device, a backflushing medium input structure and a backflushing medium output structure are arranged on a shell of the backflushing device respectively, and the backflushing medium output structure is connected with the backflushing medium conveying main pipe.

Above-mentioned coprecipitation reaction system and be used for coprecipitation reaction system's filtration enrichment facility, through the redesign to filtering concentrator inner structure, cancelled original stirring structure, the accessible makes the thick liquids flow in the stoste chamber of filtering concentrator along the central axis direction of the shell of filtering concentrator and avoids the particulate matter in the thick liquids to block up stoste chamber, and filter cake formation time on the extension filter core. In addition, the diameter of the filtering concentrator can be obviously reduced by redesigning the internal structure of the filtering concentrator, the residence time of the reaction slurry in the filtering concentrator outside the reaction kettle body is effectively reduced, the influence of the independent arrangement of the filtering concentrator on the reaction is greatly reduced, and the consistency of the granularity of the ternary precursor is ensured.

The present application will be further described with reference to the following drawings and detailed description. Additional aspects and advantages of the present application will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to assist in understanding the present application and are included to explain, by way of illustration, embodiments of the present application and not to limit the embodiments of the present application.

Fig. 1 is a schematic diagram of a co-precipitation reaction system according to an embodiment of the present disclosure.

Fig. 2 is a schematic diagram of a filter concentrator assembly of the system of fig. 1.

Fig. 3 is a schematic internal view of the filter concentrator of the assembly of fig. 2.

FIG. 4 is a schematic cross-sectional view of a filter concentrator in a co-precipitation reaction system according to an embodiment of the present disclosure.

FIG. 5 is a schematic cross-sectional view of a filter concentrator in a co-precipitation reaction system according to an embodiment of the present disclosure.

Fig. 6 is a schematic cross-sectional view of a filter concentrator in a coprecipitation reaction system according to an embodiment of the present application.

Fig. 7 is a three-dimensional structural diagram of a discharging system in a coprecipitation reaction system according to an embodiment of the present disclosure.

Fig. 8 is a three-dimensional block diagram of the system of fig. 7 at another angle.

Fig. 9 is a three-dimensional block diagram of the system of fig. 7 at another angle.

Fig. 10 is a three-dimensional block diagram of the system of fig. 7 at another angle.

Fig. 11 is a three-dimensional structure diagram of the system shown in fig. 10 after the electrical box is hidden.

Fig. 12 is a main schematic view of the system shown in fig. 7.

Detailed Description

The present application will now be described more fully hereinafter with reference to the accompanying drawings. Those of ordinary skill in the art will be able to implement the present application based on these teachings. Before describing the present application in conjunction with the drawings, it is noted that:

the technical solutions and features provided in the respective sections including the following description may be combined with each other without conflict. Furthermore, where possible, these technical solutions, technical features and related combinations may be given specific technical subject matter and are protected by the accompanying patent.

The embodiments of the application referred to in the following description are generally only some embodiments, rather than all embodiments, on the basis of which all other embodiments that can be derived by a person skilled in the art without inventive step should be considered within the scope of patent protection.

With respect to the terms and units in this specification: the terms "comprising," "including," "having," and any variations thereof in this specification and in the claims and following claims are intended to cover non-exclusive inclusions. In addition, the term "reactor" in the present description and in the corresponding claims and the relevant parts is not necessarily to be understood as a single reactor, but may also be understood as an integer comprising a main reactor and a secondary reactor, or an integer comprising a reactor and an aging reactor. Other related terms and units can be reasonably construed based on the description to provide related contents.

The applicant of the present application has developed two coprecipitation reaction systems for the preparation of ternary precursors of positive electrode materials for lithium ion secondary batteries before the present application is proposed. The following is a brief description of these two coprecipitation reaction systems in order to provide a full understanding of the present application. For convenience of description, the two coprecipitation reaction systems will be hereinafter referred to as a first coprecipitation reaction system and a second coprecipitation reaction system, respectively.

First coprecipitation reaction system

The first coprecipitation reaction system mainly comprises: a coprecipitation reaction unit and a filtration concentration unit. The filtration and concentration unit may also include a purge system as described below, if desired (depending primarily on the range of products actually sold by the applicant).

The coprecipitation reaction unit comprises a reaction kettle, the reaction kettle is provided with a shell and an inner cavity, the shell of the reaction kettle is respectively provided with a raw material feeding structure, a to-be-concentrated slurry discharging structure and a concentrated slurry backflow structure, the raw material feeding structure, the to-be-concentrated slurry discharging structure and the concentrated slurry backflow structure are respectively communicated with the inner cavity of the reaction kettle, and a stirring structure is arranged in the inner cavity of the reaction kettle.

The filtration concentration unit contains the filtration concentrator, the filtration concentrator has shell and filter core, the filter core is in form stoste chamber and clear solution chamber in the shell of filtration concentrator, be equipped with respectively on the shell of filtration concentrator and remain concentrated thick liquids feeding structure, concentrated thick liquids ejection of compact structure and clear solution ejection of compact structure, wait concentrated thick liquids feeding structure with concentrated thick liquids ejection of compact structure respectively with stoste chamber intercommunication, clear solution ejection of compact structure with clear solution chamber intercommunication.

In addition, a stirring structure is also arranged in the filtering concentrator. The stirring structure in the filtering concentrator comprises a main shaft positioned in the filtering concentrator and a stirring paddle arranged on the main shaft, and the main shaft is driven by a motor outside the filtering concentrator. Filter the filter core in the concentrator then interval arrangement peripheral at the stirring rake, can stir thick liquids when the stirring rake is rotatory, prevent that the particulate matter in the thick liquids from subsiding and prolong filter cake formation time on the filter core simultaneously.

The device comprises a to-be-concentrated slurry discharging structure, a to-be-concentrated slurry feeding structure, a concentrated slurry discharging structure, a raw material feeding structure and a clear liquid discharging structure, wherein the to-be-concentrated slurry discharging structure is used for being connected with the to-be-concentrated slurry feeding structure, the concentrated slurry discharging structure is used for being connected with the concentrated slurry backflow structure, the raw material feeding structure is used for being connected with a co-precipitation clear liquid discharging system reaction raw material supply device, and the clear liquid discharging structure is used for being connected with a clear liquid discharging system.

Above-mentioned raw materials feeding structure, treat concentrated thick liquids ejection of compact structure, concentrated thick liquids backward flow knot, treat concentrated thick liquids feeding structure, concentrated thick liquids ejection of compact structure, clear liquid ejection of compact structure can contain the pipeline interface that corresponds respectively, still is equipped with the valve on the pipeline interface when needs.

During the preparation process of the ternary precursor of the lithium ion secondary battery anode material, nickel sulfate (or nickel chloride), cobalt sulfate (or cobalt chloride) and manganese sulfate (or manganese chloride) are prepared into a mixed salt solution with a certain molar concentration, sodium hydroxide is prepared into an alkali solution with a certain molar concentration, ammonia water with a certain concentration is used as a complexing agent, the mixed salt solution, the alkali solution and the complexing agent are added into a reaction kettle at a certain flow rate through a raw material feeding structure, the stirring rate of the reaction kettle, the temperature and the pH value of reaction slurry, the reaction atmosphere (which generally requires the reaction process to be finished under the protection of nitrogen at present) and the like, so that salt and alkali are subjected to neutralization reaction to generate a ternary precursor crystal nucleus and grow gradually. In the reaction kettle operation process, the reaction raw materials are added into the reaction kettle, partial reaction slurry in the reaction kettle is pumped into the filtering concentrator, the filtering concentrator is internally provided with a filter element and is provided with a stirring structure, the reaction slurry is filtered through the filter element and then clear liquid can be output from the filtering concentrator, the clear liquid can be reused for reaction as mother liquid, and the concentrated liquid in the filtering concentrator returns to the reaction kettle through a concentrated slurry backflow structure. When filtering the concentration, the stirring rake rotation in filtering the concentrator stirs thick liquids, prevents that the particulate matter in the thick liquids from subsiding and prolongs the cake formation time of straining on the filter core.

Drawbacks of the first co-precipitation reaction system include: firstly, the internal structure design of the filter concentrator leads to larger volume of the filter concentrator, so that the reaction slurry stays in the filter concentrator outside the reaction kettle for a longer time, the reaction process is influenced by various process parameters, and once the environment changes, the reaction is influenced, so that the consistency of the reaction and the granularity of the ternary precursor is influenced when the slurry stays in the filter concentrator for a longer time. Secondly, the filter element forming time on the surface of the filter element is shorter when high-concentration slurry is treated, and the filtering flux is reduced rapidly. Thirdly, the slurry cannot be dispersed for a long time after forming a filter cake, so that the particles are agglomerated, and the consistency of the product appearance is influenced. Fourth, the tank and the stirring structure of the filtration concentrator are bulky, resulting in high manufacturing and use costs. Fifthly, the motor power of the stirring structure is high, and the energy consumption is high.

Second coprecipitation reaction system

Aiming at the problems brought by the independent arrangement of the filtering concentrator in the first coprecipitation reaction system, the filtering concentrator is cancelled in the second coprecipitation reaction system, and a filter element of the filtering concentrator is directly arranged in the reaction kettle. In this case, the reaction kettle can be called as a coprecipitation reaction and filtration concentration integrated device.

Particularly, coprecipitation reaction and concentrated integration equipment that filters contain reation kettle and the filter core of equipment together, reation kettle has shell and inner chamber, be equipped with raw materials feeding structure, concentrated thick liquids ejection of compact structure and clear liquid ejection of compact structure on reation kettle's the shell respectively, be equipped with the stirring structure in reation kettle's the inner chamber, the filter core is installed form stoste chamber and clear liquid chamber in filtering concentrator's the shell.

The inner chamber of reation kettle with stoste chamber intercommunication, raw materials feeding structure and concentrated thick liquids ejection of compact structure respectively with reation kettle's inner chamber intercommunication, raw materials feeding structure is used for being connected with codeposition reaction raw materials supply apparatus, clear liquid ejection of compact structure with clear liquid chamber intercommunication, clear liquid ejection of compact structure is used for with play clear system connection.

Because the reaction and the filtration concentration are carried out in the coprecipitation reaction and filtration concentration integrated equipment, the reaction slurry is always in the same environment, and the influence of the independent deployment of the filtration concentrator on the reaction is avoided. However, it is noted that: the coprecipitation reaction and filtration concentration integrated equipment has higher requirement on the material damage prevention stability of the filter element. If the filter element is damaged, the reaction slurry is contaminated by the material falling off from the filter element.

In addition, the second coprecipitation reaction system cannot solve the problems that the filter element forming time on the surface of the filter element is short and the filtering flux is reduced rapidly when the coprecipitation reaction and filtering concentration integrated equipment is used for treating high-concentration slurry; after the slurry forms a filter cake, the filter cake cannot be dispersed for a long time, so that the particles are agglomerated, and the consistency of the product appearance is influenced; the tank body and the stirring structure of the coprecipitation reaction and filtration concentration integrated equipment have larger volumes, so that the manufacturing and use cost is higher; the motor power of the stirring structure is large, and the energy consumption is high.

In addition, no matter the first coprecipitation reaction system or the second coprecipitation reaction system, the clear liquid filtered by the filter element needs to be output through a clear liquid outlet system. At present, a cleaning system mainly comprises a plurality of parts such as pipelines, valves, backflushing devices and the like, the parts are temporarily installed on site along with the field installation of a filter concentrator or a coprecipitation reaction and filter concentration integrated device, the construction strength is high, the time is long, and the project construction progress is influenced.

The present application thus proposes the following embodiments, which will give a corresponding solution to at least one of the problems mentioned above.

Third coprecipitation reaction system

A coprecipitation reaction system comprises a coprecipitation reaction unit and a filtering concentration unit. The filtration and concentration unit may also include a purge system as described below, if desired (depending primarily on the range of products actually sold by the applicant).

The slurry discharging structure to be concentrated is used for being connected with the slurry feeding structure to be concentrated, the concentrated slurry discharging structure is used for being connected with the concentrated slurry backflow structure, the raw material feeding structure is used for being connected with co-precipitation reaction raw material supply equipment, and the clear liquid discharging structure is used for being connected with a clear liquid discharging system.

In the filtration concentrator, the filter element has a first edge and a second edge which are perpendicular to each other, the area of the filter surface of the filter element is basically determined by the product of the length of the first edge and the length of the second edge, the direction of the length of the first edge is consistent with the direction of the central axis of the housing of the filtration concentrator, and the slurry feeding structure to be concentrated and the concentrated slurry discharging structure are respectively arranged on the housing of the filtration concentrator at positions at two ends of the central axis and are respectively communicated with two ends of the stock solution cavity.

And, if a plane perpendicular to the central axis and intersecting the filter surface of the filter element is taken as a cross section: on the cross section, the stock solution cavities are distributed in the form of a first graph, the first graph is a closed graph, the shape of the closed graph is circular, annular or polygonal, the area, except the first graph, of the cross section, which is positioned in the shell of the filtering concentrator, is basically composed of a second graph and a third graph, the clear solution cavities are distributed in the form of the second graph, the filtering materials of the filter element are distributed in the form of the third graph, and the corresponding central points of the central axis on the cross section are close to or positioned in the first graph, the second graph or the third graph.

In a first mode

Fig. 1 is a schematic diagram of a co-precipitation reaction system according to an embodiment of the present disclosure. Fig. 2 is a schematic diagram of a filter concentrator assembly of the system of fig. 1. Fig. 3 is a schematic internal view of the filter concentrator of the assembly of fig. 2. As shown in fig. 1 to 3, a coprecipitation reaction system includes a coprecipitation reaction unit (not shown) and a filtration concentration unit.

The coprecipitation reaction unit comprises a reaction kettle, the reaction kettle is provided with a shell and an inner cavity, the shell of the reaction kettle is respectively provided with a raw material feeding structure, a to-be-concentrated slurry discharging structure A and a concentrated slurry backflow structure B, the raw material feeding structure, the to-be-concentrated slurry discharging structure A and the concentrated slurry backflow structure B are respectively communicated with the inner cavity of the reaction kettle, and a stirring structure is arranged in the inner cavity of the reaction kettle.

The filtration concentration unit contains filtration concentrator 10, filtration concentrator 10 has shell 11 and filter core 12, filter core 12 is in form stoste chamber 13 and clear liquid chamber 14 in the shell 11 of filtration concentrator, be equipped with respectively on the shell 11 of filtration concentrator 10 and treat concentrated thick liquids feeding structure 15, concentrated thick liquids ejection of compact structure 16 and clear liquid ejection of compact structure 17, treat concentrated thick liquids feeding structure 15 with concentrated thick liquids ejection of compact structure 16 respectively with stoste chamber 13 intercommunication, clear liquid ejection of compact structure 17 with clear liquid chamber 14 intercommunication.

The slurry discharging structure a to be concentrated is used for being connected with the slurry feeding structure 15 to be concentrated, the concentrated slurry discharging structure 16 is used for being connected with the concentrated slurry backflow structure B, the raw material feeding structure is used for being connected with a co-precipitation reaction raw material supply device, and the clear liquid discharging structure 17 is used for being connected with the clear liquid discharging system 200.

Specifically, the filtration and concentration unit comprises N filtration and concentration assemblies 100, wherein N is an integer greater than or equal to 1, the filtration and concentration assemblies 100 are formed by connecting a plurality of filtration and concentration devices 10, and the filtration and concentration devices 10 are tubular filtration and concentration devices 10'.

The tubular filtration concentrator 10' has a tubular housing 11 and a filter element 12 having a shape and size adapted to the pipe in the housing 11, wherein an axial passage 12A is provided in the filter element 12, and the axial passage 12A constitutes the raw liquid chamber 13 or the clear liquid chamber 14.

When the axial channel 12A forms the raw liquid chamber 13, the clear liquid chamber 14 is formed between the pipe in the housing 11 and the filter element 12. When the axial channel 12A forms the clear liquid chamber 14, the raw liquid chamber 13 is formed between the pipe in the housing 11 and the filter element 12.

Furthermore, the slurry feeding structure 15 to be concentrated and the concentrated slurry discharging structure 16 of the tubular filtration concentrator 10 'in the filtration concentrator assembly 100 are sequentially connected end to end so that the stock solution cavities 13 of the tubular filtration concentrators 10' are connected in series to form a flow path, wherein the first slurry feeding structure 15 to be concentrated is connected with the slurry discharging structure a to be concentrated, and the last concentrated slurry discharging structure 16 is connected with the concentrated slurry backflow structure B.

As shown in fig. 2-3, in one embodiment, the cartridge 12 is a tubular cartridge, and thus, the axial passage 12A is the inner conduit of the tubular cartridge, which forms the feed solution chamber 13. The wall of the shell 11 of the tubular filtering concentrator 10' is provided with the clear liquid discharging structure.

With respect to the tubular cartridge described above, it can be considered that the tubular cartridge has a first edge and a second edge perpendicular to each other, wherein the first edge can be considered as a generatrix of the cylindrical surface constituted by the inner conduit of the tubular cartridge (coinciding with the direction of the central axis of the shell 11 of the tubular filtration concentrator 10'), and the second edge can be considered as a circle formed by the bottom edge or the top edge of the cylindrical surface constituted by the inner conduit of the tubular cartridge. Here, the tubular filter element has a filter area equal to the product of the length of the first edge and the length of the second edge.

The coprecipitation reaction system of the embodiment cancels the original stirring structure through redesign of the structure of the filtering concentrator, can prevent the particles in the slurry from blocking the stock solution cavity by enabling the slurry to flow in the stock solution cavity of the filtering concentrator along the central axis direction of the shell of the filtering concentrator, and prolongs the filter cake forming time on the filter element. In addition, the tubular filtering concentrator 10' can remarkably reduce the diameter of the filtering concentrator, effectively reduce the retention time of the reaction slurry in the filtering concentrator outside the reaction kettle, greatly reduce the influence of the independent arrangement of the filtering concentrator on the reaction and ensure the consistency of the granularity of the ternary precursor.

Preferably, as shown in fig. 2, the tubular filtration concentrators 10' of the filtration concentrator assembly 100 are arranged in parallel and spaced apart arrangement, and the slurry feed structure 15 to be concentrated and the concentrated slurry discharge structure 16 between adjacent tubular filtration concentrators 10' are connected by a bend 101 such that the dope chamber 13 between adjacent tubular filtration concentrators 10' is connected in series. This allows the filter concentrator assembly 100 to be more compact and reduces the space occupied by the filter concentrator assembly 100.

In addition, the elbow 101 of the filter concentrator assembly 100 is preferably horizontally disposed. This is mainly because the slurry contains solid particles, which easily cause the solid particles to completely block the elbow 101 if the elbow 101 is vertically arranged; when the bend 101 is horizontally disposed, even if solid particles are precipitated in the bend 101, they are layered in the horizontally disposed bend 101 and flow out of a certain flow space in the upper portion of the bend 101.

When the elbow 101 in the filter concentrator assembly 100 is horizontally disposed, it is apparent that the filter concentrator assembly 100 is also horizontally disposed. Thus, when the filtration and concentration unit comprises more than 2 filtration and concentration assemblies, the more than 2 filtration and concentration assemblies are arranged up and down.

Optionally, the clear liquid discharge structures 17 of different tube filter concentrators 10' in the same filter concentrator assembly 100 may be merged together and form a set of clear liquid discharge structures; the group of clear liquid discharging structures 17 corresponds to a group of filter elements 12, and the clear liquid discharging system 200 performs back flushing regeneration on the filter elements 12 of the same group at the same time according to the group of the filter elements 12.

Alternatively, the clear liquid discharge structures 17 of different tube filter concentrators 10' in different filter concentrator assemblies 100 converge together and form a set of clear liquid discharge structures; the group of clear liquid discharging structures 17 corresponds to a group of filter elements 12, and the clear liquid discharging system 200 performs back flushing regeneration on the filter elements 12 of the same group at the same time according to the group of the filter elements 12.

Specifically, as shown in FIG. 1, the clear liquid discharge structures 17 of different tube filter concentrators 10' in different filter concentrator assemblies 100 are brought together to form a set of clear liquid discharge structures. Moreover, if the different candle filter concentrators 10' in the filter concentrator assembly 100 are numbered in the order, a group of clear liquid discharge structures are connected to the same number of candle filter concentrators 10' in different candle filter concentrator assemblies 100, which facilitates subsequent control of the pressure differential between the raw liquid chamber 13 and the clear liquid chamber 14 in each candle filter concentrator 10'.

More specifically, it carries and filter core back flush pipe-line system 210 to go out clear liquid system 200, clear liquid carry and filter core back flush pipe-line system 210 contain with the clear liquid conveyer pipe 211 of the group one-to-one of filter core 12 and equally with the recoil medium conveyer pipe 212 of the group one-to-one of filter core, the output of clear liquid conveyer pipe 211 is connected with clear liquid conveying house steward 215 through the control valve 213 that one to one set up, the input of clear liquid conveyer pipe 211 is connected with the clear liquid input interface that is used for the clear liquid ejection of compact structural connection of the group of corresponding filter core, the input of recoil medium conveyer pipe 212 is connected with recoil medium conveying house steward 216 through the control valve 214 that one to one set up, the output of recoil medium conveyer pipe 212 is connected with the bypass of the clear liquid conveyer pipe of one-to-one.

In addition, the emptying system 200 further comprises a back flushing device 217, wherein a back flushing medium input structure and a back flushing medium output structure are respectively arranged on a shell of the back flushing device 217, and the back flushing medium output structure is connected with the back flushing medium conveying main pipe 216.

The clear liquid discharge system 200 can realize the delivery of clear liquid and the simultaneous back flushing regeneration of the filter elements 12 of the same group according to the groups of the filter elements 12.

In addition, a flow regulating device 102 can be arranged between each filtering concentrator assembly 100 and the slurry discharging structure to be concentrated, and a back pressure control device 218 is arranged between a control valve 213 on each clear liquid conveying pipe 211 and a clear liquid conveying main pipe 215 on each clear liquid conveying pipe 211.

The flow regulating device 102 may be a flow regulating valve. The back pressure control device 218 may also be a valve with adjustable flow rate, so that the back pressure on the clear liquid delivery pipe 211 can be adjusted by adjusting the opening degree of the valve.

Because the flow regulating device 102 is arranged between each filtering concentrator assembly 100 and the slurry discharging structure to be concentrated, the flow of the slurry in the flow passage formed by connecting the raw liquid cavities 13 in series in each filtering concentrator assembly 100 can be balanced by controlling the flow regulating device 102, so that the flow speed of the slurry on the filtering surface in each filtering concentrator assembly 100 is close, and the anti-pollution performance of the filtering surface in each filtering concentrator assembly 100 is ensured.

After the flow rates of the slurry in the flow paths formed by the raw liquid chambers 13 connected in series in each of the filter concentrator modules 100 are balanced, the pressure difference between the raw liquid chamber 13 and the clear liquid chamber 14 in the tubular filter concentrator 10' having the same number in different filter concentrator modules 100 can be made substantially the same by adjusting the back pressure control devices 218. When the pressure difference between the original liquid chamber 13 and the clear liquid chamber 14 in the tubular filtration concentrator 10' with the same serial number in different filtration concentrator assemblies 100 is approximately the same, the tubular filtration concentrator 10' with the same serial number in different filtration concentrator assemblies 100 has similar operation conditions, and when the filter elements 12 of the same group are simultaneously backflushed and regenerated according to the groups of the filter elements 12, the backflush regeneration effect on the filter elements of the tubular filtration concentrator 10' with the same serial number in different filtration concentrator assemblies 100 is more balanced.

Optionally, the coprecipitation reaction system may further include a vapor-liquid separator 103, a shell of the vapor-liquid separator 103 is provided with a vapor-liquid mixed phase input structure, a separated liquid phase output structure, and a separated gas phase output structure, respectively, the vapor-liquid mixed phase input structure is connected to the concentrated slurry discharging structure, and the separated liquid phase output structure is connected to the concentrated slurry backflow structure B.

Optionally, the coprecipitation reaction system may further include a return pipe 104, where one end of the return pipe 104 is connected to the slurry feeding structure a to be concentrated, and the other end of the return pipe 104 is connected to the concentrated slurry discharging structure; the return line 104 is provided with at least a valve and a valve in the heat exchange cooler 105.

The slurry can be returned to the filtering and concentrating unit through the return pipe 104 for further filtering and concentrating. The temperature of the slurry rises during the concentration process and can be reduced by the heat exchange cooler 105.

In addition, a feeding pump 106 is arranged between the coprecipitation reaction unit and the filtration concentration unit.

Mode two

FIG. 4 is a schematic cross-sectional view of a filter concentrator in a co-precipitation reaction system according to an embodiment of the present disclosure. FIG. 5 is a schematic cross-sectional view of a filter concentrator in a co-precipitation reaction system according to an embodiment of the present disclosure. FIG. 6 is a schematic cross-sectional view of a filter concentrator in a co-precipitation reaction system according to an embodiment of the present disclosure.

In this embodiment, as shown in fig. 4, the cartridge 12 of the previous embodiment is replaced with a multi-channel cartridge from a tubular cartridge. A plurality of said axial channels 12A are provided in the multi-channel filter element.

It is contemplated that the multi-channel cartridge also has a first edge and a second edge that are perpendicular to each other, wherein the first edge can be considered a generatrix of a cylindrical surface formed by any of the internal tubes of the multi-channel cartridge (which coincides with the direction of the central axis of the housing 11 of the tube filter concentrator 10') and the second edge can be considered a circle formed by the bottom edge or the top edge of the cylindrical surface formed by any of the internal tubes of the multi-channel cartridge. Here, the filter area of the multi-channel filter insert is equal to the product of the length of the first edge and the length of the second edge multiplied by the number of axial channels 12A.

The multi-channel cartridge has a large filtration area and, therefore, the diameter of the housing 11 of the candle filter concentrator 10' can be increased adaptively.

Mode III

In this embodiment, as shown in fig. 5, the filter element 12 is a toroidal filter element, i.e. has two filtering surfaces, an inner filtering surface and an outer filtering surface, and a raw liquid chamber 13 is arranged between the two filtering surfaces. Liquid purifying cavities 14 are arranged in the inner-layer filtering surface and between the outer-layer filtering surface and the shell 11.

It is contemplated that the loop filter element may also have a first edge and a second edge perpendicular to each other, wherein the first edge may be considered a generatrix of a cylindrical surface formed by the outer or inner filtration surface (in a direction coincident with the central axis of the housing 11 of the candle filter concentrator 10') and the second edge may be considered a circle formed by the bottom edge or the top edge of the cylindrical surface formed by the outer or inner filtration surface. The filtering area of the annular filter element is equal to the product of the length of the outer filtering surface corresponding to the first edge and the length of the second edge, and the product of the length of the inner filtering surface corresponding to the first edge and the length of the second edge.

Mode IV

As shown in fig. 6, in this embodiment, the filter element 12 is a plate-type filter element, which divides the housing 11 into a plurality of cavities, a part of which is the raw liquid cavity 13 and a part of which is the clean liquid cavity 14.

It is contemplated that the panel cartridge also has a first edge and a second edge that are perpendicular to each other, wherein the first edge can be considered the length of the panel cartridge (in a direction that coincides with the direction of the central axis of the housing 11 of the candle filter concentrator 10') and the second edge can be considered the width of the panel cartridge. The product of the length of the first edge and the length of the second edge, such as the filter area of the plate filter elements, is multiplied by the number of the plate filter elements.

In summary, the filter concentrator of the third co-precipitation reaction system can be summarized as: in the filtering concentrator, the filter element is provided with a first edge and a second edge which are perpendicular to each other, the area of a filtering surface of the filter element is basically determined by the product of the length of the first edge and the length of the second edge, the direction of the length of the first edge is consistent with the direction of a central axis of a shell of the filtering concentrator, and the slurry feeding structure to be concentrated and the concentrated slurry discharging structure are respectively arranged on the shell of the filtering concentrator at positions at two ends of the central axis and are respectively communicated with two ends of a stock solution cavity. And, if a plane perpendicular to the central axis and intersecting the filter surface of the filter element is taken as a cross section: on the cross section, the stock solution cavities are distributed in the form of a first graph, the first graph is a closed graph, the closed graph is circular, annular or polygonal, the area, except the first graph, of the cross section, which is positioned in the shell of the filter concentrator, is basically composed of a second graph and a third graph, the clear solution cavities are distributed in the form of the second graph, the filter material of the filter element is distributed in the form of the third graph, and the corresponding central point of the central axis on the cross section is close to or positioned in the first graph, the second graph or the third graph.

Fourth coprecipitation reaction system

The existing clearing system needs to be temporarily installed on site, is high in construction strength and long in time, and influences project construction progress. The effluent system adopting the integral movable effluent module can be used in any coprecipitation reaction system. When the effluent system is used in different coprecipitation reaction systems, the composition of the effluent system may differ, but the overall structure is similar.

Fig. 7 is a three-dimensional structural diagram of a discharging system in a coprecipitation reaction system according to an embodiment of the present disclosure. Fig. 8 is a three-dimensional block diagram of the system of fig. 7 from another angle. Fig. 9 is a three-dimensional block diagram of the system of fig. 7 at another angle. Fig. 10 is a three-dimensional block diagram of the system of fig. 7 at another angle. Fig. 11 is a three-dimensional structure diagram of the system shown in fig. 10 after the electrical box is hidden. Fig. 12 is a main schematic view of the system shown in fig. 7. The purge systems shown in fig. 7-12 were actually designed for the second co-precipitation reaction system described above. When the purge system is used in different co-precipitation reaction systems, the overall structure remains similar to that shown in FIGS. 7-12, but can be locally modified as desired.

As shown in fig. 7-12, the integral movable discharging module specifically comprises: frame support 220, clear liquid delivery and filter element backwash piping system 210, functional container apparatus set 230, and the like.

The frame-type support 220 includes a support base 221 and a bridge 222 disposed on the support base 221, wherein a pipe-type facility installation area 223 is formed on one side of the support base 221 located on the bridge 222, and a functional container-type facility installation area 224 is formed in the bridge 222.

Clear liquid is carried and filter core back flush pipe-line system 210 is installed pipeline class facility installing zone 223, clear liquid is carried and filter core back flush pipe-line system 210 contain with the clear liquid conveyer pipe 211 of the group one-to-one of filter core and equally with the recoil medium conveyer pipe 212 of the group one-to-one of filter core, the output of clear liquid conveyer pipe 211 is connected with clear liquid conveying house steward 215 through the control valve 213 that one-to-one set up, the input of clear liquid conveyer pipe 211 is connected with the clear liquid input interface that is used for being connected with the clear liquid ejection of compact structure of the group of corresponding filter core, the input of recoil medium conveyer pipe 212 is connected with recoil medium conveying house steward 216 through the control valve 214 that one-to-one set up, the output of recoil medium conveyer pipe 212 is connected with the bypass of the clear liquid conveyer pipe 211 of one-to-one.

The

control valves

213 and 214 may be pneumatic valves. By controlling the state of the corresponding control valve 213 and control valve 214, the operating state (filtration or backflush regeneration) of a particular group of filter elements can be controlled.

The functional container equipment group 230 is erected on the bridge 222 and located in the functional container facility installation area 224, the functional container equipment group 230 comprises a backflushing device 231, a backflushing medium input structure and a backflushing medium output structure are respectively arranged on a shell of the backflushing device 231, and the backflushing medium output structure is connected with the backflushing medium conveying main pipe 216. The backflushing medium can be either backflushing gas or backflushing liquid.

Typically, the filter cartridges are grouped at 2 or more, and thus, the clear liquid delivery tubes 211 and the backflushing media delivery tubes 212 of the clear liquid delivery and filter cartridge backflushing piping system 210 can both be horizontally and laterally spaced apart so that the clear liquid delivery and filter cartridge backflushing piping system 210 is disposed in the piping-type facility installation area 223.

Because the clear liquid conveying pipes 211 and the backflushing medium conveying pipes 212 in the clear liquid conveying and filter element backflushing pipeline system 210 can be arranged horizontally and transversely at intervals, the central axes of the clear liquid conveying pipes 211 and the central axes of the backflushing medium conveying pipes 212 connected with the clear liquid conveying pipes 211 in a one-to-one correspondence mode can be located in the same vertical plane. In this way, the overall horizontal lateral width of the clear liquid delivery and filter element backwash tubing 210 may be saved.

Because the clear liquid conveying pipes 211 and the backflushing medium conveying pipes 212 in the clear liquid conveying and filter element backflushing pipeline system 210 can be arranged at intervals along the horizontal transverse direction, the clear liquid conveying main pipe 215 can have a clear liquid conveying main pipe horizontal transverse extension section for convenient arrangement, and the output ends of the clear liquid conveying pipes 211 in the clear liquid conveying and filter element backflushing pipeline system 210 are connected with the clear liquid conveying main pipe horizontal transverse extension section through the control valves 213 which are arranged one to one.

Similarly, the back flush medium delivery manifold 216 may have a back flush medium delivery manifold horizontal lateral extension, and the output end of the back flush medium delivery pipe 212 of the clear liquid delivery and filter core back flush pipe system 210 is connected to the back flush medium delivery manifold horizontal lateral extension through the control valves 214 arranged one to one.

On this basis, the horizontal transverse extension section of the backflushing medium conveying header pipe can be positioned above the horizontal transverse extension section of the clear liquid conveying header pipe (as shown in fig. 8-9), and the backflushing medium conveying pipes 212 are positioned above the clear liquid conveying pipes 211 corresponding to one another. Therefore, the space can be saved, the pipeline arrangement is convenient, meanwhile, the recoil medium conveying pipe 212 can apply upward force to the clear liquid conveying pipe 211, and the clear liquid conveying pipe 211 can be conveniently positioned.

Thus, the whole clean liquid conveying and filter core backwashing pipeline system 210 can be supported and fixed only by mounting the clean liquid conveying pipe mounting and positioning device 217 with a simple structure on the supporting base 221 (the clean liquid conveying pipe mounting and positioning device 217 adopts a pipe clamp) and connecting the clean liquid conveying pipe 211 with the clean liquid conveying pipe mounting and positioning device 217.

On the basis of the above-described overall movable type of the emptying module, the present application also provides improvements to the overall movable type of the emptying module, which improvements can be applied to the overall movable type of the emptying module in whole (combined) or in part (separate) to achieve specific functions or to solve specific problems.

Improvements in the first aspect

As shown in fig. 7-12, a pipe view mirror 218 is installed at the input end of the clear liquid delivery pipe 211, and a clear liquid input interface for connecting with a clear liquid discharge structure of a corresponding filter element group is connected to the pipe view mirror 218.

Specifically, the input end of the clear liquid conveying pipe 211 is provided with a vertical section, the pipe view mirror 218 is a vertical pipe view mirror and is installed on the vertical section, and the clear liquid input interface is an upper port of the vertical pipe view mirror.

After the pipeline viewing mirror 218 is installed at the input end of the clear liquid conveying pipe 211, the turbidity of the clear liquid in the clear liquid conveying pipe 211 can be observed through the pipeline viewing mirror 218, so as to determine whether the filter elements of the group corresponding to the clear liquid conveying pipe 211 are penetrated, and if the penetration occurs, the control valve 213 on the clear liquid conveying pipe 211 can be closed.

Install the pipe sight glass 218 at the input of clear liquid conveyer pipe 211, not only can judge whether each group of filter core takes place to cross according to the group of filter core, reduce the investigation degree of difficulty, simultaneously, because pipe sight glass 218 is close to recoil ware 231, like this, the accessible is close to recoil and is washed pipe sight glass 218, guarantees the visibility of pipe sight glass 218.

When the input of clear solution conveyer pipe 211 has vertical section, pipeline sight glass 218 adopts vertical pipeline sight glass and installs during on the vertical section, not only conveniently observe, can effectively avoid simultaneously to cross to filter rear-view mirror 218 and take place to block up.

Improvement of the second aspect

As shown in fig. 7 to 12, a pipe facility installation area 223 is formed on one side of the supporting base 221 located on the bridge 222, a pump equipment installation area 225 is formed on the other side of the supporting base, and a pump equipment maintenance operation area 226 is reserved between the pump equipment installation area 225 and the bridge 222.

The supernatant discharging system further includes a pump unit 240, the pump unit 240 is installed in the pump equipment installation area 225 and includes a positive pump 241 and a back-up pump (not shown in the figure) which are horizontally arranged at intervals, the positive pump 241 and the back-up pump are symmetrically arranged with a plumb surface which is arranged in the same direction as the horizontal longitudinal direction as a symmetry plane, the positive pump 241 and the back-up pump are mutually connected in parallel and are selectively connected to the supernatant conveying main pipe 215 through valves respectively to form a part of the supernatant conveying main pipe.

The pump unit 240 includes a positive pump 241 and a back-up pump arranged at a horizontal interval, that is, a redundant design is adopted, so as to ensure the stability of the operation of the pump unit 240. A pump equipment maintenance operation area 226 is ingeniously reserved between the pump equipment installation area 225 and the bridge 222, so that the field maintenance of the positive pump 241 and/or the standby pump is facilitated. In addition, the positive pump 241 and the backup pump are symmetrically designed, so that the weight distribution uniformity of the whole movable type discharging module can be improved, the operation vibration of the movable type discharging module is reduced, and the influence is smaller when the positive pump 241 and the backup pump are switched.

The significance of the above-described second aspect of the improvement applied to the first coprecipitation reaction system, the second coprecipitation reaction system, and the third coprecipitation reaction system is different.

When the co-precipitation reaction system is applied to the first co-precipitation reaction system or the second co-precipitation reaction system, since the first co-precipitation reaction system or the second co-precipitation reaction system is usually provided with a feeding pump between the reaction kettle and the filter concentrator, the positive pump 241 and the backup pump can be used as the clear liquid outlet pump through the above-mentioned second aspect modification, and when the outlet of the clear liquid delivery main 215 needs to be raised (which will be described in detail later), the clear liquid is prevented from flowing backwards.

When the co-precipitation reaction system is applied to the second co-precipitation reaction system, because the first co-precipitation reaction system usually needs to adopt negative pressure to discharge clear liquid, namely a pump needs to be arranged at the downstream of a clear liquid output flow path of the filter element for pumping, at the moment, the positive pump 241 and the standby pump actually provide filtration pressure difference for the filtration and concentration operation of the co-precipitation reaction and filtration and concentration integrated equipment. At this point, it becomes more important to integrate the pump unit 240 on the integral movable purge module. In this case, the positive pump 241 and the back-up pump are preferably hose pumps.

In addition, as shown in fig. 7 to 12, the frame-type support 221 forms an electrical box mounting area on the side opposite to the pump equipment maintenance operation area 226 in both sides of the pump equipment mounting area 225; the overall movable type unclean module further comprises an electrical box 250, and the electrical box 250 is installed in the electrical box installation area.

In addition, the clear liquid delivery manifold 215 includes a lift section 215A located downstream of the positive and back-up pumps; the lifting section 215A is respectively provided with an output port of the clear liquid conveying main pipe, a cleaning liquid input port and a cleaning liquid output port; the cleaning liquid output port is connected to the backflushing medium conveying main pipe through a cleaning liquid conveying pipe 215B, and a control valve 215C is arranged on the cleaning liquid conveying pipe; an L-shaped cantilever 222A may be disposed on a side of the bridge 222 facing the pump equipment installation area 225, and a vertical section of the L-shaped cantilever 222A may respectively connect and support a horizontal section where the output port of the clear liquid conveying main 215 is located and a horizontal section where the cleaning liquid input port is located.

In addition, the fluid delivery interfaces of the functional container equipment set 230 for external connection with the integral movable purge module and the fluid delivery interfaces of the pump set 240 for external connection with the integral movable purge module are oriented in the same horizontal and lateral direction uniformly and are not obstructed by the structure of the integral movable purge module.

Improvement of the third aspect

As shown in fig. 7 to 12, on the basis of the modification of the second aspect, the functional container apparatus set 230 further includes a heat exchange cooler 232, a clear liquid channel and a cooling medium channel separated from each other by a heat exchange wall are provided in the heat exchange cooler 232, a clear liquid inlet and a clear liquid outlet respectively connected to both ends of the clear liquid channel are provided on a housing of the heat exchange cooler 232, a cooling medium inlet and a cooling medium outlet respectively connected to both ends of the cooling medium channel are further provided on a housing of the heat exchange cooler 232, and the clear liquid inlet and the clear liquid outlet are connected in series to the clear liquid conveying manifold 215 so that the clear liquid channel constitutes a part of the clear liquid conveying manifold 215. The recuperator cooler 232 may employ water as a cooling medium.

The clear liquid can be cooled by the heat exchange cooler 232, and the growth conditions of the ternary precursor particles are destroyed, so that the phenomenon that the ternary precursor particles are further generated in the clear liquid to cause the blockage of the clear liquid conveying main pipe 215, particularly the positive pump 241 and the standby pump is avoided. In addition, when the positive pump 241 and the backup pump adopt the hose pump, the heat exchange cooler 232 can protect the hose in the hose pump after cooling the clear liquid, and the service life of the hose pump is prolonged.

Further, the heat exchange cooler 232 is a vertical container, the clear liquid inlet is located at the upper end of the heat exchange cooler, the clear liquid outlet is located at the lower end of the heat exchange cooler 232, and a pipe section, located between the clear liquid outlet and the positive pump 241 and the backup pump, on the clear liquid conveying header 215 is connected with the clear liquid outlet and the positive pump 241 and the backup pump through the bottom of the pump equipment maintenance operation area 226.

After the heat exchange cooler 232 adopts a vertical container, the occupied area is saved, and the installation on the bridge frame 222 is convenient. On this basis, a clear liquid inlet is arranged at the upper end of the heat exchange cooler 232, a clear liquid outlet is arranged at the lower end of the heat exchange cooler 232, and a pipe section, which is positioned between the clear liquid outlet and the positive pump 241 and the standby pump, on the clear liquid conveying header pipe 215 connects the clear liquid outlet with the positive pump 241 and the standby pump through the bottom of the pump equipment maintenance operation area 226, so that a space as much as possible can be reserved for the pump equipment maintenance operation area 226, and the operation is convenient.

Further, the clear liquid channel is of a vertical tubular structure, the clear liquid inlet is located at the top of the heat exchange cooler 232 and is communicated with the upper port of the vertical tubular structure, and the clear liquid outlet is located at the bottom of the heat exchange cooler 232 and is communicated with the lower port of the vertical tubular structure; and the cooling medium channel is a vertical annular pipe located between the vertical tubular structure and the shell of the heat exchange cooler 232, and the cooling medium inlet and the cooling medium outlet are respectively located at the upper and lower end side portions of the vertical annular pipe.

In addition, a waste water discharge branch 219 is connected to a pipe section of the clear liquid conveying main pipe 215 between the clear liquid outlet and the positive pump 241 and the back-up pump, the waste water discharge branch 219 is located at the lowest position of the height of all liquid flow paths in the integral movable type supernatant module, and a discharge valve is arranged on the waste water discharge branch 219.

Improvement of the fourth aspect

As shown in fig. 7 to 12, the backflushing medium input structure of the backflushing device 231 includes a backflushing liquid input structure 231A and a compressed gas input structure 231B, and a backflushing liquid overflow port 231C is further provided on the housing of the backflushing device 231, the backflushing liquid overflow port 231C is connected to the output port of the clear liquid conveying main pipe 215 through a backflushing liquid overflow pipe 231D, so that the output port of the clear liquid conveying main pipe 215 is integrally higher than the backflushing liquid overflow port 231C, and a rising section 231E is provided on the backflushing liquid overflow pipe 231D. In addition, a control valve may be provided on the back flush overflow pipe 231D.

Typically, the clear liquid delivery manifold 215 comprises a lifting section 215A downstream of the clear liquid delivery manifold, and the outlet of the clear liquid delivery manifold 215 is disposed on the lifting section 215A.

Conventionally, the backflushing device 231 then uses gas backflushing or liquid backflushing, and therefore the backflushing medium input structure is either the backflushing liquid input structure 231A or the compressed gas input structure 231B. Here, the backflushing medium input structure of the backflushing device 231 includes both the backflushing liquid input structure 231A and the compressed gas input structure 231B, so that it is possible to select between gas backflushing and liquid backflushing, or to combine gas backflushing and liquid backflushing.

Based on this, this application can also adopt this kind of innovative recoil mode, namely pour into recoil liquid and compressed gas into the recoil ware 231 through recoil liquid input structure 231A and compressed gas input structure 231B respectively, like this, the inside below of recoil ware 231 is recoil liquid and the top is compressed gas to can utilize compressed gas to promote the recoil liquid fast and flow back the filter core backward, conventional liquid recoil utilizes the diaphragm pump to provide recoil power, and the liquid recoil effect of this kind of mode is limited. But after the innovative recoil mode is adopted, the recoil force is larger.

In addition, by controlling the volume of the backflushing liquid in the backflushing device 231, the volume of the backflushing liquid can be just equal to the sum of the volumes according to the sum of the volumes of the stock solution cavities of the filter element corresponding to each backflushing (for example, the volume of the backflushing liquid is controlled to be 1-1.2 times of the sum of the volumes), so that a better backflushing effect is achieved, the amount of the backflushing liquid with small effect is reduced, and energy consumption is further saved.

Therefore, in order to better control the volume of the backflushing liquid in the backflushing device 231, a backflushing liquid overflow port 231C is provided on the housing of the backflushing device 231, so as to control the liquid level height of the backflushing liquid in the backflushing device 231 and further control the volume of the backflushing liquid in the backflushing device 231. For convenience, the backwash liquid overflow port 231C is connected to the outlet port of the clear liquid delivery manifold 215 via a backwash liquid overflow pipe 231D.

When the back flush overflow port 231C is provided in the housing of the back flush device 231 and the back flush overflow port 231C is connected to the output port of the clear liquid delivery manifold 215 via the back flush overflow pipe 231D, in order to prevent the compressed gas from leaking from the back flush overflow port 231C and the back flush overflow pipe 231D, the output port of the clear liquid delivery manifold 215 is required to be entirely higher than the back flush overflow port 231C, and the back flush overflow pipe 231D is provided with the rising section 231E, so that a liquid seal can be formed in the back flush overflow pipe 231D to prevent the compressed gas from leaking.

Improvement of fifth aspect

As shown in fig. 7 to 12, the functional container equipment set further comprises a vapor-liquid separator 233, and a vapor-liquid mixed phase input structure 233A, a separated liquid phase output structure 233B and a separated gas phase output structure 233C are respectively provided on the housing of the vapor-liquid separator 233.

When the modification of the fifth aspect is applied to the third coprecipitation reaction system, the vapor-liquid separator 233 and the vapor-liquid separator 103 may be the same device, and in this case, the vapor-liquid mixed phase input structure 233A, the separated liquid phase output structure 233B, and the separated gas phase output structure 233C of the vapor-liquid separator 233 may be connected to the corresponding pipes in the manner shown in fig. 1.

When the above-described modification of the fifth aspect is applied to the first coprecipitation reaction system or the second coprecipitation reaction system, the vapor-liquid mixed phase input structure 233A of the vapor-liquid separator 233 may be communicated with the compressed gas input structure 231B of the backflusher 231 through a communicating pipe, the communicating pipe may be connected to a compressed gas source through a gas supply bypass 231D, a control valve 233D may be connected in series to the communicating pipe between the vapor-liquid mixed phase input structure 233A and the gas supply bypass 231D, and the gas supply bypass 231D may constitute a part of the compressed gas input structure 231B.

Thus, when it is necessary to release the air pressure in the backflushing device 231, the control valve 233D may be opened, and the gas-liquid two-phase in the backflushing device 231 enters the gas-liquid separator 103 for gas-liquid separation.

Preferably, the vapor-liquid mixed phase input structure 233A includes a vapor-liquid mixed phase input pipe tangential to a sidewall of the vapor-liquid separator 233, and the communicating pipe is disposed coaxially with the vapor-liquid mixed phase input pipe.

Further, the separated liquid phase output structure 233B is connected to a waste water discharge branch 219.

The contents related to the present application are explained above. Those of ordinary skill in the art will be able to implement the present application based on these teachings. All other embodiments, which can be derived by a person skilled in the art from the description above without inventive step, shall fall within the scope of patent protection.

Claims

1. A filter enrichment facility for coprecipitation reaction system which characterized in that:

the coprecipitation reaction unit comprises a reaction kettle, the reaction kettle is provided with a shell and an inner cavity, a raw material feeding structure, a slurry discharging structure to be concentrated and a concentrated slurry backflow structure are respectively arranged on the shell of the reaction kettle, the raw material feeding structure, the slurry discharging structure to be concentrated and the concentrated slurry backflow structure are respectively communicated with the inner cavity of the reaction kettle, and a stirring structure is arranged in the inner cavity of the reaction kettle;

it comprises the following steps: the filtering and concentrating unit comprises a filtering concentrator, the filtering concentrator is provided with a shell and a filter element, the filter element forms a stock solution cavity and a clear solution cavity in the shell of the filtering concentrator, a slurry to be concentrated feeding structure, a concentrated slurry discharging structure and a clear solution discharging structure are respectively arranged on the shell of the filtering concentrator, the slurry to be concentrated feeding structure and the concentrated slurry discharging structure are respectively communicated with the stock solution cavity, and the clear solution discharging structure is communicated with the clear solution cavity;

the slurry feeding structure to be concentrated is used for being connected with the slurry discharging structure to be concentrated, the concentrated slurry discharging structure is used for being connected with the concentrated slurry backflow structure, and the clear liquid discharging structure is used for being connected with a clear liquid discharging system;

in the filtering concentrator, the filter element is provided with a first edge and a second edge which are perpendicular to each other, the area of a filtering surface of the filter element is basically determined by the product of the length of the first edge and the length of the second edge, the direction of the length of the first edge is consistent with the direction of a central axis of a shell of the filtering concentrator, and the slurry feeding structure to be concentrated and the concentrated slurry discharging structure are respectively arranged on the shell of the filtering concentrator at positions at two ends of the central axis and are respectively communicated with two ends of a stock solution cavity;

if a plane which is perpendicular to the central axis and intersects with the filtering surface of the filter element is taken as a cross section, then: on the cross section, the stock solution cavities are distributed in the form of a first graph, the first graph is a closed graph, the shape of the closed graph is circular, annular or polygonal, the area, except the first graph, of the cross section, which is positioned in the shell of the filtering concentrator, is basically composed of a second graph and a third graph, the clear solution cavities are distributed in the form of the second graph, the filtering materials of the filter element are distributed in the form of the third graph, and the corresponding central points of the central axis on the cross section are close to or positioned in the first graph, the second graph or the third graph.

2. The filtration concentrator as defined in claim 1, wherein: the filtering and concentrating unit comprises N filtering and concentrating device components, wherein N is an integer more than or equal to 1, the filtering and concentrating device components are formed by connecting a plurality of filtering and concentrating devices, and the filtering and concentrating devices are tubular filtering and concentrating devices;

the tubular filtering concentrator is provided with a tubular shell and a filter element, the shape and the size of the filter element are matched with those of a pipeline in the shell, an axial channel is arranged in the filter element, and the axial channel forms the stock solution cavity or the clear solution cavity;

when the axial channel forms the stock solution cavity, the clear solution cavity is formed between the pipeline in the shell and the filter element, and when the axial channel forms the clear solution cavity, the stock solution cavity is formed between the pipeline in the shell and the filter element;

thereby tubular filtration concentrator among the filtration concentrator subassembly treat concentrated thick liquids feeding structure and concentrated thick liquids ejection of compact structure end to end connection in proper order make these tubular filtration concentrator's stoste chamber establish ties and be a flow path, treat concentrated thick liquids feeding structure for first among the flow path with treat concentrated thick liquids ejection of compact structural connection, concentrated thick liquids ejection of compact structure at end with concentrated thick liquids backflow structure is connected.

3. The filtration concentrator of claim 2, wherein: and the wall of the shell of the tubular filtering concentrator is provided with the clear liquid discharging structure.

4. The filtration concentrator as defined in claim 2, wherein: the tubular filtering concentrators in the filtering concentrator assembly are arranged in parallel at intervals, and a slurry feeding structure to be concentrated and a concentrated slurry discharging structure between the adjacent tubular filtering concentrators are connected through an elbow, so that stock solution cavities between the adjacent tubular filtering concentrators are connected in series.

5. The filtration concentration apparatus of claim 4, wherein: the elbow in the filtering concentrator component is horizontally arranged.

6. The filtration concentrator of claim 5, wherein: the filtration concentration unit comprises more than 2 filtration concentrator components, and the more than 2 filtration concentrator components are arranged up and down.

7. The filtration concentrator as defined in claim 2, wherein: the clear liquid discharging structures of different tubular filtering concentrators in the same filtering concentrator component are converged together to form a group of clear liquid discharging structures, or the clear liquid discharging structures of different tubular filtering concentrators in different filtering concentrator components are converged together to form a group of clear liquid discharging structures; the clear liquid discharging structure corresponds to a group of filter elements, and the clear liquid discharging system performs back flushing regeneration on the filter elements of the same group according to the groups of the filter elements.

8. The filtration concentrator as defined in claim 7, wherein: the clear liquid outlet system comprises a clear liquid conveying and filter element backwashing pipeline system, the clear liquid conveying and filter element backwashing pipeline system comprises clear liquid conveying pipes which are in one-to-one correspondence with the groups of the filter elements and backwashing medium conveying pipes which are also in one-to-one correspondence with the groups of the filter elements, the output ends of the clear liquid conveying pipes are connected with a clear liquid conveying main pipe through one-to-one arranged control valves, the input ends of the clear liquid conveying pipes are connected with clear liquid input interfaces which are used for being connected with clear liquid discharging structures of the groups of the corresponding filter elements, the input ends of the backwashing medium conveying pipes are connected with the backwashing medium conveying main pipe through one-to-one arranged control valves, and the output ends of the backwashing medium conveying pipes are connected with bypasses of the clear liquid conveying pipes which are in one-to-one correspondence; the discharging system further comprises a backflushing device, a backflushing medium input structure and a backflushing medium output structure are arranged on a shell of the backflushing device respectively, and the backflushing medium output structure is connected with the backflushing medium conveying main pipe.

9. The filtration concentrator as defined in claim 8, wherein: when the clear liquid discharging structures of different tubular filtering concentrators in different filtering concentrator components are converged together to form a group of clear liquid discharging structures, a flow regulating device is arranged between each filtering concentrator component and the slurry discharging structure to be concentrated, and a back pressure control device is arranged between a control valve on each clear liquid conveying pipe and a clear liquid conveying main pipe;

and/or the recoil medium input structure of the recoil device comprises a recoil liquid input structure and a compressed gas input structure, a recoil liquid overflow port is further arranged on the shell of the recoil device, the recoil liquid overflow port is connected to the output port of the clear liquid conveying main pipe through a recoil liquid overflow pipe, the output port of the clear liquid conveying main pipe is integrally higher than the recoil liquid overflow port, and a rising section is arranged on the recoil liquid overflow pipe.

10. The filtration concentrator as defined in claim 1, wherein: the device comprises a vapor-liquid separator, wherein a vapor-liquid mixed phase input structure, a separated liquid phase output structure and a separated gas phase output structure are respectively arranged on a shell of the vapor-liquid separator, the vapor-liquid mixed phase input structure is connected with a concentrated slurry discharging structure, and the separated liquid phase output structure is connected with a concentrated slurry backflow structure;

and/or a return pipe is included, one end of the return pipe is connected with the slurry feeding structure to be concentrated, and the other end of the return pipe is connected with the concentrated slurry discharging structure; the return pipe is at least provided with a valve and a valve in the heat exchange cooler.