Automatic continuous exchange system for Y-type molecular sieve ion exchange

Abstract

The utility model relates to the technical field of molecular sieves, in particular to an automatic continuous exchange system for Y-type molecular sieve ion exchange. Comprising a cross-linking unit which comprises a cross-linking reaction kettle and is used for carrying out ammonium ion and optional rare earth ion exchange on a NaY molecular sieve to obtain a cross-linking material and discharging the cross-linking material from a cross-linking material output end; the first baking slurry unit is communicated with the first mixed material output end and is used for filtering, washing, drying, baking and pulping the first mixed material into first baking Y-type molecular sieve slurry and discharging the first baking Y-type molecular sieve slurry through the first baking Y-type molecular sieve slurry output end; the secondary exchange unit is communicated with the primary baked Y-type molecular sieve slurry output end and is used for sequentially carrying out ammonium ion exchange and rare earth ion exchange on the primary baked Y-type molecular sieve slurry to obtain a secondary exchange material and discharging the secondary exchange material from the secondary exchange material output end; and the automatic metering unit comprises flow concentration automatic metering controllers arranged at the input ends and / or output ends of the first exchange unit, the pulping unit and the second exchange unit.

Description

Technical Field

[0001] This utility model relates to the field of molecular sieve technology, specifically to an automatic continuous exchange system for Y-type molecular sieve ion exchange. Background Technology

[0002] Y-type molecular sieves possess a unique framework structure, excellent hydrothermal stability, and high catalytic activity and selectivity, making them widely applicable as active components in solid acid catalysts for catalytic cracking. To prevent heavy oil molecules from coating the catalyst surface and forming coke deposits that accelerate catalyst deactivation, other positive ions (rare earth ions, H+ ions, etc.) must be used. + NH 4+ (etc.) exchange most of the Na + The exchange process transforms the material into HY, REHY, and REY type molecular sieves, enabling them to exhibit solid acid characteristics and serve as active components in catalytic cracking catalysts. This exchange process takes place in a closed exchange vessel. To ensure safe, continuous, and efficient molecular sieve production, various process parameters must be maintained within specific ranges, necessitating intervention in the production process. To better reduce manual labor, ensure safety, and stabilize product quality, the Y-type molecular sieve exchange process must be automated and continuous. Compared to foreign countries, my country's automated continuous molecular sieve production technology is not yet fully mature. However, in recent years, the development of industrial automation instrumentation technology has received increasing attention from domestic molecular sieve manufacturers, leading to varying degrees of intelligent assistance in domestic molecular sieve production equipment of the same type.

[0003] CN202356102U discloses a pulping system for continuous production of modified NaY molecular sieves, comprising a first batching vessel, a second batching vessel, a third batching vessel, and a continuous reaction vessel. The system is characterized by an exchange solution buffer tank added between the third batching vessel and the continuous reaction vessel. The exchange solution buffer tank is connected to the top of both the third batching vessel and the continuous reaction vessel via pipelines, and its bottom is connected to the third batching vessel via pipelines and a centrifugal pump. The beneficial effects of this system are: in the continuous ion exchange process, the addition of a high-level exchange solution buffer tank and the use of overflow feeding eliminate the impact of flow instability caused by centrifugal pump pressure fluctuations. After optimization, the flow rates of each stream in the continuous exchange process are stabilized, resulting in highly stable control parameters of the PLC system. However, for molecular sieve slurries with high concentrations and viscosity, the overflow feeding method can easily lead to poor slurry flowability and pipeline blockage, resulting in poor production continuity.

[0004] CN219816277U discloses a high-efficiency continuous exchange system for Y-type molecular sieve ion exchange, comprising an exchange kettle and an intermediate kettle, wherein the exchange kettle comprises an exchange kettle body, an exchange kettle stirrer, six feed lines and two discharge lines, and the intermediate kettle comprises an intermediate kettle body, an intermediate kettle stirrer, two feed lines and one discharge line. Metered NaY molecular sieve slurry, rare earth chloride solution, ammonium salt solution, chemical water, hydrochloric acid and low-pressure steam are simultaneously added to the exchange kettle, the pH value of the reaction system is controlled by adding hydrochloric acid, the reaction temperature is controlled by adding low-pressure steam, and the ion exchange reaction is carried out under the stirring action of the stirrer. The exchange reaction product is transported to the intermediate kettle through the pipeline, and the intermediate kettle continuously discharges into the next section, so that the continuous, stable and efficient ion exchange process can be realized. However, the fluctuation of the concentration of the molecular sieve slurry easily causes the adjustment of the flow of other solutions to be not timely, which causes quality fluctuation; at the same time, the system does not involve oxalic acid, sulfuric acid and other solutions; at the same time, ammonium sulfate and rare earth solution are added to the exchange kettle, which has the quality risk of producing rare earth sulfate precipitate.

[0005] CN104275215A discloses a molecular sieve microwave continuous ion exchange method, which mainly solves the technical problems of long exchange time, discontinuity and low utilization rate of exchange solution in the existing molecular sieve ion exchange. The present application comprises the following steps: a) sodium type molecular sieve enters the exchange kettle from the upper part of the exchange kettle; b) the ion exchange solution is fed from the lower part of the exchange kettle and contacts with the molecular sieve in the kettle; the weight concentration of the ion to be exchanged in the ion exchange solution is 0.01-50%; c) microwave radiation is used to exchange the molecular sieve and the ion exchange solution in the exchange kettle, the time of the ion exchange solution passing through the molecular sieve on the microwave action surface is 1 second-10 minutes, the exchange temperature is from 0°C to 180°C, and the total exchange time is 0.00028-20 hours; d) the solution after ion exchange flows out of the device from the upper part of the exchange kettle; the ion-exchanged molecular sieve is discharged from the lower part of the exchange kettle. The technical scheme solves the problem and can be applied to the industrial production of molecular sieve ion exchange. However, the method needs microwave radiation equipment and needs additional external energy supply.

[0006] CN216499413U discloses a continuous ion exchange reaction device. The device comprises a feed unit, a reaction unit and a tail gas treatment unit; wherein the reaction unit comprises a preheater, two or more stages of ion exchange reactors, a cooler and a product tank connected in series; the ion exchange reactor is used to provide ion exchange hot-pressing conditions, so that the reactant is preheated in the preheater, then sequentially undergoes ion exchange reaction under the hot-pressing conditions in each stage of the ion exchange reactor, and then is cooled in the cooler; the tail gas treatment unit comprises a tail gas washing tank for washing and discharging the tail gas of the ion exchange reaction; a back pressure valve is arranged on the material pipeline between the product tank and the tail gas washing tank. The continuous ion exchange reaction device has the effect of improving the ion exchange degree. However, the device uses hot-pressing conditions of 100-220 DEG C and 0.6-3.0 MPa in use, and cannot exchange under normal temperature and pressure conditions.

[0007] Primary and secondary exchange of Y-type molecular sieve is a key link affecting crystallinity, sodium oxide content and rare earth oxide content of the molecular sieve. Main problems existing in the link include: (1) multiple operation steps, low continuity, intermittent tank exchange operation in metering, dosing and sampling links; (2) small fault tolerance space, high precision requirement in the exchange process; (3) large labor intensity of workers; and (4) solid oxalic acid, ammonium sulfate solution and other raw materials need to be added in the SOY molecular sieve exchange, and the current raw materials are added intermittently, mainly relying on manual counting and dosing, and the exchange effect is affected if the addition is not timely. Practical new type content

[0008] The utility model aims at overcoming the problems of small fault tolerance space, low efficiency and large labor intensity of workers in the prior art. An automatic continuous exchange system for ion exchange of Y-type molecular sieve is provided. The system has the advantages of stable product quality, high efficiency and low labor intensity of workers.

[0009] In order to achieve the above-mentioned purpose, the utility model provides an automatic continuous exchange system for ion exchange of Y-type molecular sieve, comprising:

[0010] A primary exchange unit, comprising a primary exchange reactor, is used for ammonium ion and optional rare earth ion exchange of NaY molecular sieve to obtain primary exchange material and discharge from a primary exchange material output end;

[0011] A calcined and beaten pulp unit, which is communicated with the primary exchange material output end, is used for filtering, washing, drying, calcining and beating of the primary exchange material to obtain calcined Y-type molecular sieve pulp and discharge through a calcined Y-type molecular sieve pulp output end;

[0012] A secondary exchange unit, which is communicated with the calcined Y-type molecular sieve pulp output end, is used for ammonium ion exchange and rare earth ion exchange of the calcined Y-type molecular sieve pulp to obtain secondary exchange material and discharge from a secondary exchange material output end; and

[0013] The automatic metering unit comprises a flow concentration automatic metering controller arranged at the input end and / or output end of each of the first exchange unit, the beating unit and the second exchange unit.

[0014] In some embodiments, the first exchange unit further comprises a NaY molecular sieve feeding pipeline, a first ammonium salt solution feeding pipeline, a first water feeding pipeline and a first pH adjuster feeding pipeline in communication with the first exchange reactor, and a first agitator arranged in the first exchange reactor, for continuously introducing the NaY molecular sieve, the ammonium salt solution, the water and the pH adjuster into the first exchange reactor to perform ammonium ion exchange under the agitation of the first agitator to obtain the first exchange material and discharge the first exchange material from the first exchange material output end.

[0015] In some embodiments, the automatic metering unit comprises a flow concentration automatic metering controller arranged on each of the feeding pipeline, the first ammonium salt solution feeding pipeline, the first water feeding pipeline and the first pH adjuster feeding pipeline, and a pH analyzer arranged on the first exchange reactor.

[0016] In some embodiments, the first exchange unit further comprises a first rare earth source solution feeding pipeline in communication with the first exchange reactor, for continuously introducing the first rare earth source solution into the first exchange reactor to perform ammonium ion and rare earth ion exchange with the NaY molecular sieve, the ammonium salt solution and the water under the agitation of the first agitator to obtain the first exchange material and discharge the first exchange material from the first exchange material output end.

[0017] In some embodiments, the automatic metering unit comprises a flow concentration automatic metering controller arranged on the first rare earth source solution feeding pipeline.

[0018] In some embodiments, the calcined and beaten material unit comprises a filter washer, a dryer, a calciner and a beater; the filter washer is in communication between the first exchange material output end and the dryer, so as to be capable of supplying the first exchange material into the filter washer to perform filtration and washing, then supplying the first exchange material into the dryer to perform drying to obtain dried material and discharge the dried material from the dried material output end; the dryer is connected to the calciner through the dried material output end, so as to be capable of supplying the dried material into the calciner to perform calcination to obtain calcined material and discharge the calcined material from the calcined material output end; the calciner is connected to the beater through the calcined material output end, so as to be capable of supplying the calcined material into the beater to perform beating to obtain a calcined Y-type molecular sieve slurry and discharge the calcined Y-type molecular sieve slurry through the calcined Y-type molecular sieve slurry output end.

[0019] In some embodiments, the beater is provided with a second water feeding pipeline; and a second agitator is arranged in the beater, for performing beating of the water and the calcined material under the agitation of the second agitator to obtain the calcined Y-type molecular sieve slurry.

[0020] In some embodiments, the two-exchange unit comprises an intermediate tank, a first exchange kettle and a second exchange kettle; the intermediate tank is connected between the output end of the calcined Y-type molecular sieve slurry and the first exchange kettle, and is used to introduce the calcined Y-type molecular sieve slurry in the calcined slurry unit into the intermediate tank for stirring to obtain mixed exchange slurry and continuously discharge the mixed exchange slurry from the mixed exchange slurry output end; the first exchange kettle is connected with the intermediate tank through the mixed exchange slurry output end, and is used to continuously introduce the mixed exchange slurry to obtain ammonium exchange slurry by ammonium exchange and discharge the ammonium exchange slurry from the ammonium exchange slurry output end; the second exchange kettle is connected with the first exchange kettle through the ammonium exchange slurry output end, and is used to introduce the ammonium exchange slurry to obtain rare earth exchange slurry by rare earth ion exchange and discharge the rare earth exchange slurry from the rare earth exchange slurry output end.

[0021] In some embodiments, the two-exchange unit further comprises: a calcined Y-type molecular sieve slurry collection pipeline connected between the output end of the calcined Y-type molecular sieve slurry and the intermediate tank, a third stirrer arranged in the intermediate tank and used to stir the calcined Y-type molecular sieve slurry introduced into the intermediate tank to obtain mixed exchange slurry and discharge the mixed exchange slurry from the mixed exchange slurry output end; a first exchange kettle feed pipeline connected between the mixed exchange slurry output end and the first exchange kettle, a third water feed pipeline, a second ammonium salt solution feed pipeline, an oxalic acid solution feed pipeline and a second pH adjuster feed pipeline arranged on the first exchange kettle, a fourth stirrer arranged in the first exchange kettle and used to continuously introduce the mixed exchange slurry into the first exchange kettle and perform ammonium exchange on the mixed exchange slurry, the ammonium salt solution, the oxalic acid and the pH adjuster under the stirring of the fourth stirrer to obtain ammonium exchange slurry and discharge the ammonium exchange slurry from the ammonium exchange slurry output end; a second exchange kettle collection pipeline connected between the ammonium exchange slurry output end and the second exchange kettle, a second rare earth source solution feed pipeline arranged on the second exchange kettle, and a fifth stirrer arranged in the second exchange kettle and used to perform rare earth ion exchange on the second rare earth source solution and the ammonium exchange slurry introduced into the first exchange kettle to obtain rare earth exchange slurry and discharge the rare earth exchange slurry from the rare earth exchange slurry output end.

[0022] In some embodiments, the automatic metering unit comprises: flow concentration automatic metering controllers arranged on the calcined Y-type molecular sieve slurry collection pipeline, the first exchange kettle feed pipeline, the third water feed pipeline, the second ammonium salt solution feed pipeline, the oxalic acid solution feed pipeline, the second pH adjuster feed pipeline, the second exchange kettle collection pipeline and the second rare earth source solution feed pipeline, respectively, and a pH analyzer arranged on the first exchange kettle.

[0023] By the above technical solution, at least the following beneficial effects are achieved:

[0024] (1) Stable product quality: the automatic continuous exchange system ensures the consistency of product quality. The traditional batch production method is easily affected by operating conditions, resulting in large fluctuations in product quality. However, the method of the present application has higher exchange stability after implementation, and the fluctuation range of the rare earth content of Y-type molecular sieve is reduced by 30%.

[0025] (2)High efficiency: through the automatic continuous exchange system, the production efficiency is improved significantly, the time required by the traditional intermittent method is saved, the system can reduce the start and stop of the pump and other equipment, the opening and closing of the valve, the sampling and metering link, the continuous operation of the system is ensured, and the daily output is increased by 5.67%.

[0026] (3) Reduce labor intensity: rely on automatic metering unit to realize automatic metering and control, realize continuous feeding, ion exchange and discharging, greatly reduce manual operation link, and reduce labor intensity. BRIEF DESCRIPTION OF DRAWINGS

[0027] Figure 1 It is the overall view of the automatic continuous exchange system of Y-type molecular sieve ion exchange disclosed in the embodiment of the utility model.

[0028] MARKING OF THE DRAWINGS

[0029] 101, NaY molecular sieve feeding pipeline 102, first ammonium salt solution feeding pipeline

[0030] 103, first water feeding pipeline 104, first reaction kettle

[0031] 105, first stirrer 106, first rare earth source solution feeding pipeline

[0032] 107, first pH regulator feeding pipeline 201, filter washer

[0033] 202, dryer 203, calciner

[0034] 204, beater 205, second water feeding pipeline

[0035] 206, second stirrer 1, calcined Y-type molecular sieve slurry collecting pipeline

[0036] 2, intermediate tank 3, first exchange kettle feeding pipeline

[0037] 4, third water feeding pipeline 5, first exchange kettle

[0038] 6, second ammonium salt solution feeding pipeline 7, oxalic acid solution feeding pipeline

[0039] 8, second pH regulator feeding pipeline 9, second exchange kettle collecting pipeline

[0040] 10, material transfer pump 11, second rare earth source solution feeding pipeline

[0041] 12, second exchange kettle 13, third stirrer

[0042] 14, fourth stirrer 15, fifth stirrer

[0043] 16. Intermediate tank transfer pump Detailed Implementation

[0044] In this invention, unless otherwise stated, directional terms such as "up," "down," "left," "right," "inner," and "outer" are used only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention. When the absolute position of the described object changes, the relative positional relationship may also change accordingly.

[0045] The primary and secondary ion exchange processes of Y-type molecular sieves are crucial steps affecting the crystallinity, sodium oxide content, and rare earth oxide content of the sieves. Current Y-type molecular sieve preparation methods are primarily intermittent, suffering from low operational tolerance and low yield. To address the problems of limited error tolerance, low efficiency, and high labor intensity in the existing Y-type molecular sieve exchange process, this invention provides an automated continuous ion exchange system for Y-type molecular sieves, such as... Figure 1 As shown, it includes: a primary exchange unit, comprising a primary exchange reactor 104, used for ammonium ion and optionally rare earth ion exchange of NaY molecular sieve to obtain primary exchange material, which is discharged from the primary exchange material output end; a calcination and slurry unit, connected to the primary exchange material output end, used for filtering, washing, drying, calcining, and slurrying the primary exchange material into a calcined Y-type molecular sieve slurry, which is discharged from the calcined Y-type molecular sieve slurry output end; a secondary exchange unit, connected to the calcined Y-type molecular sieve slurry output end, used for sequentially exchanging the calcined Y-type molecular sieve slurry with ammonium ions and rare earth ions to obtain secondary exchange material, which is discharged from the secondary exchange material output end; and an automatic metering unit, comprising an automatic flow concentration metering controller installed at each input end and / or output end of the primary exchange unit, the slurry unit, and the secondary exchange unit. The aforementioned automated continuous ion exchange system for Y-type molecular sieves continuously performs primary and secondary ion exchange operations on the Y-type molecular sieves. Simultaneously, an automatic metering unit controls the flow rate and concentration of each material, achieving an automated, continuous, and stable ion exchange process. The term "optional rare earth ions" refers to the ability to introduce or omit rare earth source solutions during the secondary ion exchange, depending on requirements.

[0046] In some embodiments, the exchange unit further includes a NaY molecular sieve feed line 101, a first ammonium salt solution feed line 102, a first water feed line 103, and a first pH adjuster feed line 107 connected to the exchange reactor 104, as well as a first stirrer 105 disposed in the exchange reactor 104, for continuously introducing NaY molecular sieve, ammonium salt solution, water, and pH adjuster into the exchange reactor 104 for ammonium ion exchange under the stirring of the first stirrer 105 to obtain an exchange material and discharge it from the exchange material output end.Figure 1 NaY molecular sieve, ammonium salt solution, water and pH regulator are introduced into the first exchange reactor 104 continuously and simultaneously to obtain the first exchange material, and then the first exchange material is discharged from the first exchange material output end. The NaY molecular sieve, ammonium salt solution, water and pH regulator can also be introduced at different times, or the NaY molecular sieve, ammonium salt solution and water can be introduced first, and then the pH regulator is introduced. The addition amount of the NaY molecular sieve, ammonium salt solution and water is adjusted according to the required amount of ammonium ion exchange. In the art, the weight ratio of the NaY molecular sieve, ammonium salt and water is generally controlled to be 1:0.2-0.5:5-10 on a dry basis. In the process of the first exchange, the pH regulator in the art is generally selected from sulfuric acid or hydrochloric acid to control the pH of the system to be 3-5.5.

[0047] In the utility model, the NaY molecular sieve from the upstream can exist in the form of dry powder or be dispersed in water and introduced into the first exchange reactor 104 from the NaY molecular sieve feeding pipeline 101. In the art, the solid content is generally 40-50wt%.

[0048] In some embodiments, the automatic metering unit comprises flow concentration automatic metering controllers arranged on the feeding pipeline 101, the first ammonium salt solution feeding pipeline 102, the first water feeding pipeline 103 and the first pH regulator feeding pipeline 107 respectively, and a pH analyzer arranged on the first exchange reactor 104, which is used to control the amount of the NaY molecular sieve, ammonium salt solution, water and pH regulator introduced into the first exchange reactor 104. A sampling port is arranged on the first exchange reactor 104 and connected to the pH analyzer. When the pH value reaches the set value, the introduction of the pH regulator is stopped, and finally the first exchange material is supplied to the second exchange unit.

[0049] In some embodiments, the first exchange unit further comprises a first rare earth source solution feeding pipeline 106 in communication with the first exchange reactor 104, which is used to continuously introduce the first rare earth source solution into the first exchange reactor 104 to exchange the ammonium ion and rare earth ion with the NaY molecular sieve, ammonium salt solution and water under the stirring of the first stirrer 105 to obtain the first exchange material, and then the first exchange material is discharged from the first exchange material output end. Figure 1In the first ion exchange process, the NaY molecular sieve, the ammonium salt solution, water, the pH regulator, and the first rare earth source solution are introduced into the first ion exchange reactor 104 simultaneously and continuously to exchange the ammonium ions to obtain the first ion exchange material, and then the first ion exchange material is discharged from the first ion exchange material output end. The NaY molecular sieve, the ammonium salt solution, water, the pH regulator, and the first rare earth source solution can also be introduced into the first ion exchange reactor 104 at different times, that is, the NaY molecular sieve, the ammonium salt solution, water, and the first rare earth source solution can be introduced first, and then the pH regulator is introduced. The amounts of the NaY molecular sieve, the ammonium salt solution, water, and the first rare earth source solution are adjusted according to the amounts of the ammonium ions and the rare earth ions to be exchanged. In general, the first rare earth source is a rare earth chloride, and the weight ratio of the NaY molecular sieve, the ammonium salt, water, and the rare earth source is 1:0.2-0.5:5-10:0-0.07 on a dry basis in the art. In the first ion exchange process, the pH regulator is generally selected from sulfuric acid or hydrochloric acid to control the pH of the system to be 3-5.5.

[0050] In some embodiments, the automatic metering unit includes a flow concentration automatic metering controller arranged on the first rare earth source solution feed pipeline 106 to control the introduction of the first rare earth source solution.

[0051] In some embodiments, as shown in FIG. 2, the first ion exchange material output end is connected to a filter washer 201, a dryer 202, a calciner 203, and a beater 204 in sequence. Figure 1 The filter washer 201 is connected to the dryer 202 to supply the first ion exchange material to the filter washer 201 for filtration and washing and then to the dryer 202 for drying to obtain dried material and discharge the dried material from a dried material output end. The dryer 202 is connected to the calciner 203 through the dried material output end to supply the dried material to the calciner 203 for calcination to obtain calcined material and discharge the calcined material from a calcined material output end. The calciner 203 is connected to the beater 204 to supply the calcined material to the beater 204 for beating to obtain a calcined Y-type molecular sieve slurry and discharge the calcined Y-type molecular sieve slurry from a calcined Y-type molecular sieve slurry output end. The first ion exchange material is sequentially subjected to filtration, washing, drying, calcination, and beating to obtain the calcined Y-type molecular sieve slurry. The filter washer, the dryer, the calciner, and the beater are all conventional devices in the art.

[0052] In some embodiments, as shown in FIG. 2, the beater 204 is provided with a second water feed pipeline 205. A second agitator 206 is arranged in the beater 204 to beat the water and the calcined material under the agitation of the second agitator 206 to obtain the calcined Y-type molecular sieve slurry. Figure 1

[0053] In some embodiments, as shown in FIG. 2, the beater 204 is provided with a second water feed pipeline 205. A second agitator 206 is arranged in the beater 204 to beat the water and the calcined material under the agitation of the second agitator 206 to obtain the calcined Y-type molecular sieve slurry. Figure 1 ​As shown, the two-exchange unit comprises the intermediate tank 2, the first exchange kettle 5 and the second exchange kettle 12; the intermediate tank 2 is communicated between the output end of the calcined Y-type molecular sieve slurry and the first exchange kettle 5, and is used for introducing the calcined Y-type molecular sieve slurry in the calcined slurry unit into the intermediate tank 2 for stirring to obtain mixed exchange slurry and continuously discharging from the mixed exchange slurry output end; the first exchange kettle 5 is communicated with the intermediate tank 2 through the mixed exchange slurry output end, and is used for continuously introducing the mixed exchange slurry for ammonium exchange to obtain ammonium exchange slurry and discharging from the ammonium exchange slurry output end; the second exchange kettle 12 is communicated with the first exchange kettle 5 through the ammonium exchange slurry output end, and is used for introducing the ammonium exchange slurry for rare earth ion exchange to obtain rare earth exchange slurry and discharging from the rare earth exchange slurry output end. The materials in the system are continuously introduced and discharged, the calcined Y-type molecular sieve slurry is first stirred in the intermediate tank 2, which can avoid the problem that the concentration fluctuation of the calcined Y-type molecular sieve slurry directly introduced into the first exchange kettle 5 causes other solution flow adjustment not timely, the mixed exchange slurry in the intermediate tank 2 is first introduced into the first exchange kettle 5 for ammonium exchange, and then is introduced into the second exchange kettle 12 for rare earth ion exchange, which can avoid the quality risk of rare earth salt precipitation.

[0054] In some embodiments, as shown, Figure 1 As shown, the two-exchange unit further comprises: a calcined Y-type molecular sieve slurry collecting pipeline 1 communicated between the calcined Y-type molecular sieve slurry output end and the intermediate tank 2, a third stirrer 13 arranged in the intermediate tank 2 and used for stirring the calcined Y-type molecular sieve slurry introduced into the intermediate tank 2 to obtain mixed exchange slurry and discharging from the mixed exchange slurry output end; a first exchange kettle feeding pipeline 3 communicated between the mixed exchange slurry output end and the first exchange kettle 5, a third water feeding pipeline 4, a second ammonium salt solution feeding pipeline 6, an oxalic acid solution feeding pipeline 7 and a second pH adjuster feeding pipeline 8 arranged on the first exchange kettle 5, a fourth stirrer 14 arranged in the first exchange kettle 5 and used for continuously introducing the mixed exchange slurry into the first exchange kettle 5 to perform ammonium exchange with the ammonium salt solution, the oxalic acid and the pH adjuster under the stirring of the fourth stirrer 14 to obtain ammonium exchange slurry and discharging from the ammonium exchange slurry output end; a second exchange kettle collecting pipeline 9 communicated between the ammonium exchange slurry output end and the second exchange kettle 12, a second rare earth source solution feeding pipeline 11 arranged on the second exchange kettle 12, and a fifth stirrer 15 arranged in the second exchange kettle 12 and used for performing rare earth ion exchange between the second rare earth source solution and the ammonium exchange slurry introduced into the first exchange kettle 5 to obtain rare earth exchange slurry and discharging from the rare earth exchange slurry output end. Figure 1In the prior art, the slurry of the calcined Y-type molecular sieve is introduced into the intermediate tank 2, and the mixed exchange slurry is obtained by mixing and stirring through the third stirrer 13. The mixed exchange slurry, the ammonium salt solution, the oxalic acid solution and water are continuously introduced into the first exchange kettle 5, and the pH of the system is generally controlled to be 2.5-3.5 by a pH regulator. The ammonium exchange slurry is continuously introduced into the second exchange kettle 12, and the rare earth ion exchange is carried out under the stirring of the fifth stirrer 15. In the prior art, the weight ratio of the slurry of the calcined Y-type molecular sieve, the second rare earth source, the oxalic acid and water is generally controlled to be 1:0.02-0.3:0.05-0.08:5-10 on a dry basis.

[0055] In some embodiments, as shown in Figure 1 The automatic metering unit includes flow concentration automatic metering controllers arranged on the slurry pipeline 1 of the calcined Y-type molecular sieve, the first exchange kettle feed pipeline 3, the third water feed pipeline 4, the second ammonium salt solution feed pipeline 6, the oxalic acid solution feed pipeline 7, the second pH regulator feed pipeline 8, the second exchange kettle collection pipeline 9 and the second rare earth source solution feed pipeline 11 respectively, and a pH analyzer arranged on the first exchange kettle 5, so as to control the amount of the slurry of the calcined Y-type molecular sieve, the mixed exchange slurry, water, the ammonium salt solution and the oxalic acid solution introduced into the first exchange kettle 5, control the amount of the ammonium exchange slurry and the second rare earth source solution introduced into the second exchange kettle 12, and stop the introduction of the pH regulator after the pH value of the first exchange kettle 5 reaches the set value.

[0056] In the system of the utility model, in order to make each material enter or exit, pumps can be arranged on each pipeline according to needs to realize the introduction or exit of the material, for example, the intermediate tank transfer pump 16 is arranged on the first exchange kettle feed pipeline 3, and the transfer pump 10 is arranged on the second exchange kettle collection pipeline 9. In addition, the flow of the flow concentration automatic metering controller arranged on the corresponding pipeline can be controlled and metered through the flow concentration automatic metering controller, or can be controlled through the frequency converter of the corresponding pump.

[0057] In some embodiments, as shown in Figure 1 The automatic continuous exchange system for the ion exchange of the Y-type molecular sieve can include the following steps:

[0058] NaY zeolite is metered by the flow concentration automatic metering controller on the NaY zeolite feed pipeline 101, the ammonium salt solution is metered by the flow concentration automatic metering controller on the first ammonium salt solution feed pipeline 102, the water is metered by the flow concentration automatic metering controller on the first water feed pipeline 103, and then they are continuously fed into a first exchange reactor 104 at the same time. The pH adjuster (usually sulfuric acid or hydrochloric acid) is metered by the flow concentration automatic metering controller on the first pH adjuster feed pipeline 107 and then continuously fed into the first exchange reactor 104. The ammonium ion exchange is carried out under the stirring of the first stirrer 105 to obtain a first exchange material. The pH of the first exchange material is monitored by the pH analyzer arranged on the first exchange reactor 104. When the pH value reaches the set value, the introduction of the pH adjuster is stopped.

[0059] The first exchange material is sequentially introduced into the filter washer 201, the dryer 202, and the calciner 203 to sequentially carry out filtration, washing, drying, and calcination to obtain a calcined material.

[0060] The calcined material enters the beater 204, and the water enters the beater 204 from the second water feed pipeline 205. The beater slurry of the calcined Y-type zeolite is obtained under the stirring of the second stirrer 206.

[0061] The beater slurry of the calcined Y-type zeolite is fed into the intermediate tank 2 and mixed and stirred by the third stirrer 13 to obtain a mixed exchange slurry. The flow concentration automatic metering controller arranged on the beater slurry of the calcined Y-type zeolite feed pipeline 1 is used to control the slurry flow and concentration of the beater slurry of the calcined Y-type zeolite in real time.

[0062] The mixed exchange slurry is metered by the flow concentration automatic metering controller on the first exchange reactor feed pipeline 3 and then continuously enters the first exchange reactor 5 through the intermediate tank transfer pump 16. The ammonium salt solution, the oxalic acid solution, the water, and the pH adjuster (usually sulfuric acid or hydrochloric acid) are continuously introduced into the first exchange reactor 5 after being metered by the flow concentration automatic metering controllers arranged on the second ammonium salt solution feed pipeline 6, the oxalic acid solution feed pipeline 7, the third water feed pipeline 4, and the second pH adjuster feed pipeline 8 in real time. The ammonium exchange is carried out to obtain an ammonium exchange slurry. The pH of the ammonium exchange slurry is monitored by the pH analyzer arranged on the first exchange reactor 5. When the pH value reaches the set value, the introduction of the pH adjuster is stopped.

[0063] The ammonium ion exchange slurry is metered in real time by an automatic flow and concentration metering controller on the receiving pipeline 9 of the second exchange vessel. Controlled by the frequency converter of the transfer pump 10, it enters the second exchange vessel 12. Simultaneously, the automatic flow and concentration metering controller on the feeding pipeline 11 of the second rare earth source solution meteres the second rare earth source solution into the second exchange vessel 12. This solution undergoes rare earth ion exchange with the ammonium ion exchange slurry under the stirring of the fifth stirrer 15, resulting in a rare earth exchange slurry, which then proceeds to the next process. This next process involves conventional solid-liquid separation, washing, and drying processes.

[0064] In some embodiments, such as Figure 1 As shown, the entire automated continuous ion exchange system for Y-type molecular sieves may include the following steps:

[0065] After the NaY molecular sieve is metered by the automatic flow and concentration metering controller on the NaY molecular sieve feed line 101, the ammonium salt solution is metered by the automatic flow and concentration metering controller on the first ammonium salt solution feed line 102, the first rare earth source solution feed line 106, and the water is metered by the automatic flow and concentration metering controller on the first water feed line 103. Simultaneously, they are continuously fed into a primary reaction vessel 104. A pH adjuster (generally sulfuric acid or hydrochloric acid) is metered by the automatic flow and concentration metering controller on the first pH adjuster feed line 107 and continuously fed into the primary reaction vessel 104. Under the stirring of the first stirrer 105, ammonium ions and rare earth ions are exchanged to obtain a primary material. The pH of the primary material is monitored by a pH analyzer installed on the primary reaction vessel 104. Once the pH value reaches the set value, the introduction of the pH adjuster is stopped.

[0066] A batch of material is sequentially introduced into a filter washer 201, a dryer 202, and a calciner 203 for filtration, washing, drying, and calcination to obtain calcined material.

[0067] The calcined material enters the pulper 204, and water enters the pulper 204 from the second water inlet pipe 205. The pulping is carried out under the stirring of the second agitator 206 to obtain a calcined Y-type molecular sieve slurry.

[0068] The slurry of a 1-baked Y-type molecular sieve is collected into an intermediate tank 2 and mixed and stirred by a third agitator 13 to obtain a mixed exchange slurry. The flow rate and concentration of the 1-baked Y-type molecular sieve slurry are controlled and measured in real time by an automatic flow and concentration metering controller installed on the 1-baked Y-type molecular sieve slurry collection pipeline 1.

[0069] The mixed exchange slurry is continuously introduced into the first exchange kettle 5 through the intermediate tank transfer pump 16 after metering by the flow concentration automatic metering controller on the first exchange kettle feed pipeline 3. The ammonium salt solution, the oxalic acid solution, the water and the pH adjusting agent (generally sulfuric acid or hydrochloric acid) are continuously introduced into the first exchange kettle 5 to obtain the ammonium exchange slurry after metering by the flow concentration automatic metering controllers arranged on the second ammonium salt solution feed pipeline 6, the oxalic acid solution feed pipeline 7 and the third water feed pipeline 4 and the second pH adjusting agent feed pipeline 8 in real time, and the pH of the ammonium exchange slurry is monitored by the pH analyzer arranged on the first exchange kettle 5, and the introduction of the pH adjusting agent is stopped when the pH reaches the set value.

[0070] The ammonium exchange slurry is introduced into the second exchange kettle 12 through the flow concentration automatic metering controller on the second exchange kettle receiving pipeline 9 to control the flow and concentration of the slurry in real time, and the second rare earth source solution is introduced into the second exchange kettle 12 to exchange with the ammonium exchange slurry under the stirring of the fifth stirrer 15 to obtain the rare earth exchange slurry, and the next process is entered, wherein the next process is the conventional solid-liquid separation, washing and drying process in the art.

[0071] The present application will be described in detail below through examples.

[0072] In the examples and comparative examples, the NaY molecular sieve (also referred to as NaY zeolite) used is provided by Qilu Branch Company of Sinopec Catalyst Co., Ltd., the sodium oxide content is 13.5 wt%, the framework silicon aluminum ratio (molar ratio of SiO2 / Al2O3) = 4.6, the unit cell constant is 2.470 nm, and the relative crystallinity is 90%; the rare earth chloride solution is provided by Qilu Branch Company of Sinopec Catalyst Co., Ltd., and the rare earth chloride content is 100 g / L; the oxalic acid solution is provided by Qilu Branch Company of Sinopec Catalyst Co., Ltd., and the oxalic acid content is 10 wt%; and the ammonium salt solution is provided by Qilu Branch Company of Sinopec Catalyst Co., Ltd., and the ammonium sulfate content is 14 wt%. The specifications of the chemical reagents used in the examples and comparative examples are not particularly specified, and they are of chemical purity.

[0073] In the present application, the crystallinity is determined by the standard method of RIPP145 90; n(SiO2) / n(Al2O3), i.e. the silicon aluminum ratio, is calculated from the content of silicon oxide and aluminum oxide, the content of silicon oxide and aluminum oxide is determined by the standard method of GB / T 30905 2014; the specific surface area is determined by the standard method of GB5816; and the element content of Y-type molecular sieve is determined by X-ray fluorescence spectroscopy.

[0074] Example 1

[0075] NaY molecular sieve is metered by flow concentration automatic metering controller on NaY molecular sieve feed pipeline 101 (about 1 t (dry basis) cake is added per hour, solid content is 46%, sodium oxide content is 13.5% by weight, industrial product of Sinopec Catalyst Qilu Branch, inlet and outlet balance), ammonium salt solution is metered by flow concentration automatic metering controller on first ammonium salt solution feed pipeline 102, water is metered by flow concentration automatic metering controller on first water feed pipeline 103, and then they are continuously introduced into a first exchange reactor 104 at the same time. pH regulator (sulfuric acid) is metered by flow concentration automatic metering controller on first pH regulator feed pipeline 107 and is continuously introduced into the first exchange reactor 104, and ammonium ion exchange is carried out under the stirring of a first stirrer 105 to obtain a first exchange material (temperature is room temperature, stirring time is 45 min). The pH of the first exchange material is monitored by a pH analyzer arranged on the first exchange reactor 104, and the introduction of the pH regulator is stopped when the pH value reaches the set value 3.5. The weight ratio of NaY molecular sieve to ammonium salt to water is 1:0.3:7 on a dry basis.

[0076] The first exchange material is sequentially introduced into a filter washer 201, a dryer 202 and a calciner 203 to sequentially carry out filtration, washing, drying and calcination to obtain a calcined material.

[0077] The calcined material enters a beater 204, and water from a second water feed pipeline 205 enters the beater 204 at the same time. The beater 204 is stirred by a second stirrer 206 to carry out beater to obtain a calcined Y-type molecular sieve slurry. The weight ratio of the calcined material to water is 1:6.

[0078] The calcined Y-type molecular sieve slurry is fed into the intermediate tank 2 and mixed by the third stirrer 13 to obtain mixed exchange slurry, and the flow and concentration of the calcined Y-type molecular sieve slurry are controlled in real time by the flow and concentration automatic metering controller arranged on the calcined Y-type molecular sieve slurry feeding pipeline 1 (about 1 t (dry basis) is added per hour); the mixed exchange slurry is continuously fed into the first exchange kettle 5 through the intermediate tank transfer pump 16 after being metered by the flow and concentration automatic metering controller on the first exchange kettle feeding pipeline 3; the ammonium salt solution, the oxalic acid solution, the water and the pH adjuster (sulfuric acid) are continuously fed into the first exchange kettle 5 after being metered in real time by the flow and concentration automatic metering controllers arranged on the second ammonium salt solution feeding pipeline 6, the oxalic acid solution feeding pipeline 7 and the third water feeding pipeline 4 and the second pH adjuster feeding pipeline 8, to carry out ammonium exchange to obtain ammonium exchange slurry, and the pH of the ammonium exchange slurry is monitored by the pH analyzer arranged on the first exchange kettle 5, and the introduction of the pH adjuster is stopped when the pH value reaches 3.0; the flow and concentration of the ammonium exchange slurry are controlled in real time by the flow and concentration automatic metering controller on the second exchange kettle feeding pipeline 9, and the slurry is fed into the second exchange kettle 12 through the frequency converter control of the transfer pump 10, and the flow and concentration automatic metering controller on the second rare earth source solution feeding pipeline 11 controls the chlorinated rare earth solution to be fed into the second exchange kettle 12 to carry out rare earth ion exchange with the ammonium exchange slurry under the stirring of the fifth stirrer 15 to obtain rare earth exchange slurry, which is fed into the next process, and the weight ratio of NaY molecular sieve, chlorinated rare earth, oxalic acid and water is 1:0.035:0.06:7 (dry basis). The next process is a conventional solid-liquid separation, washing and drying process in the art.

[0079] Compared with Comparative Example 1, the daily output is increased by about 5.67%, and the product qualified rate is increased by about 11%.

[0080] Example 2

[0081] NaY molecular sieve is metered by flow concentration automatic metering controller on NaY molecular sieve feed pipeline 101 (about 1 t (dry basis) cake is added per hour, solid content is 46%, sodium oxide content is 13.5% by weight, industrial product of Sinopec Catalyst Qilu Branch, inlet and outlet balance), ammonium salt solution is metered by flow concentration automatic metering controller on first ammonium salt solution feed pipeline 102, water is metered by flow concentration automatic metering controller on first water feed pipeline 103, and then they are continuously introduced into a first exchange reactor 104 at the same time. pH regulator (sulfuric acid) is metered by flow concentration automatic metering controller on first pH regulator feed pipeline 107 and is continuously introduced into the first exchange reactor 104, and ammonium ion exchange is carried out under the stirring of a first stirrer 105 to obtain a first exchange material (temperature is room temperature, stirring time is 45 min). The pH of the first exchange material is monitored by a pH analyzer arranged on the first exchange reactor 104, and the introduction of the pH regulator is stopped when the pH value reaches the set value 3.5. The weight ratio of NaY molecular sieve to ammonium salt to water is 1:0.3:7 on a dry basis.

[0082] The first exchange material is sequentially introduced into a filter washer 201, a dryer 202 and a calciner 203 to sequentially carry out filtration, washing, drying and calcination to obtain a calcined material.

[0083] The calcined material enters a beater 204, and water from a second water feed pipeline 205 enters the beater 204 at the same time. The beater 204 is stirred by a second stirrer 206 to carry out beater to obtain a calcined Y-type molecular sieve slurry. The weight ratio of the calcined material to water is 1:6.

[0084] The calcined Y-type molecular sieve slurry is fed into the intermediate tank 2 and mixed by the third stirrer 13 to obtain mixed exchange slurry, and the flow and concentration of the calcined Y-type molecular sieve slurry are controlled by the flow and concentration automatic metering controller arranged on the calcined Y-type molecular sieve slurry feeding pipeline 1 in real time (about 1 t (dry basis) is added per hour); the mixed exchange slurry is continuously fed into the first exchange kettle 5 through the intermediate tank transfer pump 16 after being metered by the flow and concentration automatic metering controller arranged on the first exchange kettle feeding pipeline 3; the ammonium salt solution, the oxalic acid solution, the water and the pH adjuster (sulfuric acid) are continuously fed into the first exchange kettle 5 after being metered by the flow and concentration automatic metering controllers arranged on the second ammonium salt solution feeding pipeline 6, the oxalic acid solution feeding pipeline 7 and the third water feeding pipeline 4 and the second pH adjuster feeding pipeline 8 in real time, to carry out ammonium exchange to obtain ammonium exchange slurry, and the pH of the ammonium exchange slurry is monitored by the pH analyzer arranged on the first exchange kettle 5, and the introduction of the pH adjuster is stopped when the pH value reaches 3.0; the flow and concentration of the ammonium exchange slurry are controlled by the flow and concentration automatic metering controller arranged on the second exchange kettle feeding pipeline 9 in real time, and the ammonium exchange slurry is fed into the second exchange kettle 12 through the frequency converter control of the transfer pump 10, and the flow and concentration automatic metering controller arranged on the second rare earth source solution feeding pipeline 11 controls the metering of the chlorinated rare earth solution into the second exchange kettle 12 to carry out rare earth ion exchange with the ammonium exchange slurry under the stirring of the fifth stirrer 15 to obtain rare earth exchange slurry, which is fed into the next process, and the weight ratio of NaY molecular sieve, chlorinated rare earth, oxalic acid and water is 1:0.15:0.06:7 on a dry basis. The next process is a conventional solid-liquid separation, washing and drying process in the art.

[0085] The daily output is similar to that of Example 1.

[0086] Example 3

[0087] NaY molecular sieve is metered by flow concentration automatic metering controller on NaY molecular sieve feed pipeline 101 (about 1 t (dry basis) cake is added per hour, solid content is 46%, sodium oxide content is 13.5% by weight, industrial product of Sinopec Catalyst Qilu Branch, inlet and outlet material balance), ammonium salt solution is metered by flow concentration automatic metering controller on first ammonium salt solution feed pipeline 102, first rare earth source solution is metered by flow concentration automatic metering controller on first rare earth source solution feed pipeline 106, water is metered by flow concentration automatic metering controller on first water feed pipeline 103, and they are continuously introduced into a first exchange reactor 104 at the same time. pH adjuster (sulfuric acid) is continuously introduced into the first exchange reactor 104 under the stirring of a first stirrer 105 after being metered by flow concentration automatic metering controller on first pH adjuster feed pipeline 107, to exchange ammonium ions and rare earth ions to obtain a first exchange material (temperature is room temperature, stirring time is 45 min), and the pH of the first exchange material is monitored by a pH analyzer arranged on the first exchange reactor 104, and the introduction of the pH adjuster is stopped when the pH value reaches 4.5. The weight ratio of NaY molecular sieve, rare earth chloride, ammonium salt and water is 1:0.05:0.24:7 based on dry basis.

[0088] The first exchange material is sequentially introduced into a filter washer 201, a dryer 202 and a calciner 203 to sequentially perform filtration, washing, drying and calcination to obtain a calcined material.

[0089] The calcined material enters a beater 204, and water from a second water feed pipeline 205 enters the beater 204 under the stirring of a second stirrer 206 to perform beating to obtain a calcined Y-type molecular sieve slurry. The weight ratio of the calcined material and water is 1:6.

[0090] The one-baking Y-type molecular sieve slurry is fed into the intermediate tank 2 through the third stirrer 13 to obtain mixed exchange slurry, and the flow and concentration of the one-baking Y-type molecular sieve slurry are controlled in real time by the flow and concentration automatic metering controller arranged on the one-baking Y-type molecular sieve slurry feeding pipeline 1 (about 1 t (dry basis) is added per hour); the in-out balance is controlled, and the mixed exchange slurry is continuously fed into the first exchange kettle 5 through the intermediate tank transfer pump 16 after being controlled by the flow and concentration automatic metering controller arranged on the first exchange kettle feeding pipeline 3; the ammonium salt solution, the oxalic acid solution, the water, and the pH adjuster (sulfuric acid) are continuously fed into the first exchange kettle 5 after being controlled in real time by the flow and concentration automatic metering controllers arranged on the second ammonium salt solution feeding pipeline 6, the oxalic acid solution feeding pipeline 7, the third water feeding pipeline 4, and the second pH adjuster feeding pipeline 8 to perform ammonium exchange to obtain ammonium exchange slurry, and the pH of the ammonium exchange slurry is monitored by the pH analyzer arranged on the first exchange kettle 5, and the introduction of the pH adjuster is stopped when the pH value reaches 2.9; the flow and concentration of the ammonium exchange slurry are controlled in real time by the flow and concentration automatic metering controller arranged on the second exchange kettle feeding pipeline 9, and the ammonium exchange slurry is fed into the second exchange kettle 12 through the frequency converter control of the transfer pump 10, and the flow and concentration automatic metering controller arranged on the second rare earth source solution feeding pipeline 11 controls the chlorinated rare earth solution to be fed into the second exchange kettle 12 to perform rare earth ion exchange with the ammonium exchange slurry under the stirring of the fifth stirrer 15 to obtain rare earth exchange slurry, which is fed into the next process, and the weight ratio of NaY molecular sieve to chlorinated rare earth, oxalic acid, and water is 1:0.13:0.07:7 (dry basis). The next process is a conventional solid-liquid separation, washing, and drying process in the art.

[0091] The daily output is similar to that of Example 1.

[0092] Comparative Example 1

[0093] According to the weight ratio of NaY molecular sieve to ammonium salt and water of 1:0.3:7 (dry basis), the NaY molecular sieve (artificial sampling analysis concentration is about 48 wt%), the ammonium salt solution, and the water are added into the reaction kettle, and then the pH adjuster (sulfuric acid) is added, wherein the pH value in the reaction kettle is continuously analyzed by artificial sampling, and the introduction of the pH adjuster is stopped when the pH value reaches the set value 3.5 to obtain one-baking material;

[0094] The one-baking material is sequentially filtered, washed, dried, and baked to obtain baked material; then the baked material and water are added into the beater according to the weight ratio of 1:6 to perform beating to obtain one-baking Y-type molecular sieve slurry;

[0095] The calcined Y type molecular sieve slurry, the ammonium salt solution, the oxalic acid solution and water are added into a reaction kettle for mixing and stirring, then a pH regulator (sulfuric acid) is added for stirring, and when the pH value in the reaction kettle is 3, the adding of the pH regulator is stopped by manual sampling, the rare earth chloride solution is continuously added for stirring to obtain a rare earth exchange slurry, and the next process is entered, the weight ratio of the NaY molecular sieve to the rare earth chloride, the oxalic acid and water is 1:0.035:0.06:7 on a dry basis, and the next process is a conventional solid-liquid separation, washing, drying and the like.

[0096] The preferred embodiments of the present application are described in detail above with reference to the drawings, but the present application is not limited thereto. Within the technical concept of the present application, the technical solution of the present application can be subjected to various simple modifications, including the combination of various specific technical features in any suitable manner. In order to avoid unnecessary repetition, the present application will not be described again for various possible combination manners. However, these simple modifications and combinations should also be regarded as the disclosed content of the present application, and all belong to the protection scope of the present application.

Claims

1. An automatic continuous ion exchange system for ion exchange of Y-type molecular sieves, characterized by, The system comprises: a first exchange unit, the first exchange unit comprising a first exchange reactor (104) for NaY molecular sieve to exchange ammonium ions and optionally rare earth ions to obtain a first exchange material and discharge from a first exchange material outlet; a first calcined and slurried material unit, the first calcined and slurried material unit being in communication with the first exchange material outlet, for the first exchange material to be filtered, washed, dried, calcined, and slurried to obtain a first calcined Y-type molecular sieve slurry and discharge from a first calcined Y-type molecular sieve slurry outlet; a second exchange unit, the second exchange unit being in communication with the first calcined Y-type molecular sieve slurry outlet, for the first calcined Y-type molecular sieve slurry to be sequentially exchanged with ammonium ions and rare earth ions to obtain a second exchange material and discharge from a second exchange material outlet; and an automatic metering unit, the automatic metering unit comprising flow and concentration automatic metering controllers arranged at respective inputs and / or outputs of the first exchange unit, the first calcined and slurried material unit, and the second exchange unit.

2. The automatic continuous exchange system according to claim 1, wherein the first exchange unit further comprises a NaY molecular sieve feed line (101), a first ammonium salt solution feed line (102), a first water feed line (103), a first pH adjuster feed line (107), and a first agitator (105) arranged in the first exchange reactor (104), which are in communication with the first exchange reactor (104), for the NaY molecular sieve, the ammonium salt solution, the water, and the pH adjuster to be continuously introduced into the first exchange reactor (104) to exchange ammonium ions under agitation of the first agitator (105) to obtain the first exchange material and discharge from the first exchange material outlet.

3. The automatic continuous exchange system according to claim 2, wherein the automatic metering unit comprises flow and concentration automatic metering controllers arranged on the NaY molecular sieve feed line (101), the first ammonium salt solution feed line (102), the first water feed line (103), and the first pH adjuster feed line (107), respectively, and a pH analyzer arranged on the first exchange reactor (104).

4. The automatic continuous exchange system according to claim 2, wherein the first exchange unit further comprises a first rare earth source solution feed line (106) in communication with the first exchange reactor (104), for the first rare earth source solution to be continuously introduced into the first exchange reactor (104) to exchange ammonium ions and rare earth ions with the NaY molecular sieve, the ammonium salt solution, and the water under agitation of the first agitator (105) to obtain the first exchange material and discharge from the first exchange material outlet.

5. The automatic continuous exchange system according to claim 4, wherein the automatic metering unit comprises a flow and concentration automatic metering controller arranged on the first rare earth source solution feed line (106).

6. The automatic continuous exchange system according to claim 1, wherein The calcined slurry unit comprises a filter washer (201), a dryer (202), a calciner (203) and a beater (204); the filter washer (201) is communicated between an intermediate material output end and the dryer (202) to enable the supply of intermediate material into the filter washer (201) for filtration and washing, then into the dryer (202) for drying to obtain dried material and discharge from a dried material output end; The calciner (203) is communicated to the beater (204) through a calcined material output end to enable the supply of calcined material into the beater (204) for beating to obtain a calcined Y-type molecular sieve slurry and discharge through a calcined Y-type molecular sieve slurry output end.

7. The automatic continuous exchange system according to claim 6, characterized in that, The beater (204) is provided with a second water feeding pipeline (205); and a second agitator (206) is arranged in the beater (204) to beat the water and the calcined material under the agitation of the second agitator (206) to obtain the calcined Y-type molecular sieve slurry.

8. The automatic continuous exchange system according to claim 1, characterized in that, The secondary exchange unit comprises an intermediate tank (2), a first exchange kettle (5) and a second exchange kettle (12); the intermediate tank (2) is communicated between a calcined Y-type molecular sieve slurry output end and the first exchange kettle (5) to introduce the calcined Y-type molecular sieve slurry in the calcined slurry unit into the intermediate tank (2) for agitation to obtain mixed exchange slurry and continuously discharge from a mixed exchange slurry output end; the first exchange kettle (5) is communicated with the intermediate tank (2) through the mixed exchange slurry output end to continuously introduce the mixed exchange slurry for ammonium exchange to obtain ammonium exchange slurry and discharge from an ammonium exchange slurry output end; and the second exchange kettle (12) is communicated with the first exchange kettle (5) through the ammonium exchange slurry output end discharge to introduce the ammonium exchange slurry for rare earth ion exchange to obtain rare earth exchange slurry and discharge from a rare earth exchange slurry output end.

9. The automatic continuous exchange system according to claim 8, characterized in that, The secondary exchange unit further comprises: a calcined Y-type molecular sieve slurry collecting pipeline (1) communicated between the calcined Y-type molecular sieve slurry output end and the intermediate tank (2), a third agitator (13) arranged in the intermediate tank (2) to agitate the calcined Y-type molecular sieve slurry introduced into the intermediate tank (2) to obtain the mixed exchange slurry and discharge from the mixed exchange slurry output end; A first exchange kettle feed line (3) is connected between the mixed exchange slurry output end and the first exchange kettle (5). A third water feed line (4), a second ammonium salt solution feed line (6), an oxalic acid solution feed line (7) and a second pH adjuster feed line (8) are arranged on the first exchange kettle (5). A fourth stirrer (14) is arranged in the first exchange kettle (5). The mixed exchange slurry is continuously introduced into the first exchange kettle (5) and the ammonium exchange is carried out under the stirring of the fourth stirrer (14) to obtain the ammonium exchange slurry. The ammonium exchange slurry is discharged from the ammonium exchange slurry output end. A second exchange kettle collection line (9) is connected between the ammonium exchange slurry output end and the second exchange kettle (12). A second rare earth source solution feed line (11) is arranged on the second exchange kettle (12). A fifth stirrer (15) is arranged in the second exchange kettle (12). The second rare earth source solution and the ammonium exchange slurry introduced into the first exchange kettle (5) are subjected to the rare earth ion exchange to obtain the rare earth exchange slurry. The rare earth exchange slurry is discharged from the rare earth exchange slurry output end.

10. The automatic continuous exchange system according to claim 9, wherein the automatic metering unit comprises a flow concentration automatic metering controller arranged on the calcined Y-type molecular sieve slurry collection line (1), the first exchange kettle feed line (3), the third water feed line (4), the second ammonium salt solution feed line (6), the oxalic acid solution feed line (7), the second pH adjuster feed line (8), the second exchange kettle collection line (9) and the second rare earth source solution feed line (11) respectively, and a pH analyzer arranged on the first exchange kettle (5). ​

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