CN108536909B - Multi-component linkage extraction separation process design system and design method - Google Patents

Multi-component linkage extraction separation process design system and design method Download PDF

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CN108536909B
CN108536909B CN201810183244.6A CN201810183244A CN108536909B CN 108536909 B CN108536909 B CN 108536909B CN 201810183244 A CN201810183244 A CN 201810183244A CN 108536909 B CN108536909 B CN 108536909B
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程福祥
廖春生
吴声
王嵩龄
刘艳
张玻
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CHINA MINMETALS(BEIJING)RESEARCH INSTITUTE
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Abstract

The invention belongs to the technical field of solvent extraction separation, and relates to a multi-component linkage extraction separation process design system and a design method. The design system comprises a data input module, a flow calculation module, a progression calculation module and a result output module, wherein the flow calculation module is used for constructing a full separation flow chart according to components to be separated and the number of the components, which are input by the data input module, and calculating the minimum extraction amount, the minimum washing amount, the total material flow at two ends and the component flow rate of each component required by each separation unit in the full separation flow chart from top to bottom in a hierarchy mode, and adjacent separation units of the same hierarchy adopt the input and output material total flow rates and the component flow rates of each component in a linkage stage after the outlets are linked. By utilizing the design system and the design method, the workload of determining and optimizing process parameters can be reduced when the design system and the design method are used for the process design of the rare earth linkage extraction separation process, and the theoretical minimum extraction amount and the theoretical minimum washing amount can be accurately judged according to the full.

Description

Multi-component linkage extraction separation process design system and design method
Technical Field
The invention belongs to the technical field of solvent extraction separation, and relates to a multi-component linkage extraction separation process design system and a design method.
Background
Mr. xu-Photonic constitution of Beijing university in the last 70 th century proposed the cascade extraction theory for rare earth separation, developed the computer static design and dynamic simulation technology of cascade extraction, and realized the 'one-step amplification' of rare earth separation process design parameters to industrial scale production, thereby promoting the rapid development of rare earth separation industry in China. In the beginning of the century, in order to further reduce the consumption of chemical auxiliary materials and the emission of pollutants in the multi-component total separation process, a linkage extraction separation technology is developed, and the technology becomes a basic technology in the rare earth separation industry in China at present.
The core of the linkage extraction separation technology is that different separation units in the multi-component separation process are transversely or longitudinally connected, so that loaded organic phase or aqueous phase material solution generated by some separation units is supplied to other separation units to be used as extraction organic phases or washing liquid, thereby avoiding the repeated consumption of chemical reagents by each separation unit and achieving the purpose of reducing the total consumption of the process. The process requires the linkage operation of the separation units, so the process is called linkage extraction separation technology.
The coupled extraction separation technique is also referred to as fuzzy coupled extraction technique. The study of the new fuzzy linkage extraction process of Baotou mixed rare earth ore (see: research of the new fuzzy linkage extraction process of Baotou mixed rare earth ore, rare metals and hard alloy, 45(3):1-4, 2017), Zhao Zhihua (see: comparison of economic and technical indexes of the linkage extraction and separation process of Baoyibo rare earth ore, Chinese rare earth academy, 34(1):70-76, 2016) describes the characteristic of fuzzy linkage extraction, designs several LaCePrNd four-component linkage extraction processes, and compares and analyzes the economy of the LaCePrNd four-component linkage extraction processes with the traditional process. However, all these designs of coupled extraction schemes are not optimized with respect to chemical reagent consumption. Containing A1、A2、…、AtThe optimized linkage extraction full-separation process of t components is shown in fig. 2, wherein the separation unit represented by each box needs to be linked with other separation units in an outlet or feeding stage connection mode, so that the total chemical reagent consumption of the process is reduced to the maximum extent.
The optimized design of rare earth separation process is mainly based on the cascade extraction theory proposed by Mr. xu-xiong (supra) (see: xu-xiong, rare earth (supra), Beijing: Metallurgical Press, 1995). The minimum extraction and wash amounts represent the theoretical minimum consumption of chemical reagents required for a given separation process, and approaching the theoretical minimum extraction and wash amounts as close as possible is an important matter of the design of the rare earth separation process. Early cascade extraction theories gave theoretical minimum extract and minimum wash formulas for two-component separations, but were not accurately applicable to multi-component separation systems. Wu Yin et al developed an accurate algorithm for solving the static design of a multi-component and multi-outlet fractional extraction system and designed dynamic simulation software to verify the design results (see Wu Yin et al, Chinese rare earth academy 22(1): 17&22(2):171, 2004).
Although these methods can be used for the process design of the rare earth linkage extraction separation process, the optimized process parameters need to be preferentially determined from a large number of calculation results, so that the workload is large, and the basis for judging whether the selected result is the theoretical minimum value is lacked.
Disclosure of Invention
The invention aims to provide a multi-component linkage extraction separation process design system, which can reduce the workload of determining and optimizing process parameters and can judge the theoretical minimum extraction amount and the minimum washing amount fully and accurately according to the process design for the multi-component linkage extraction separation process.
In order to achieve the purpose, in a basic embodiment, the invention provides a multi-component linkage extraction separation process design system, which comprises a data input module, a flow calculation module, a stage calculation module and a result output module;
the data input module is used for inputting the component fraction t to be separated and the component A to be separated1、 A2、…、AtCoefficient of separation between components to be separated
Figure BDA0001589519590000021
The requirements for impurities and calculation accuracy in the final product are met; wherein t is more than or equal to 3, i is more than or equal to 1 and less than or equal to t-1, and the separation is carried outThe components in the used extraction system are A according to the sequence of easy to be extracted and difficult to be extracted1、A2、…、At；
The flow calculation module is used for constructing a full separation flow chart according to the components to be separated and the number of the components to be separated, which are input by the data input module, and calculating the minimum extraction amount, the minimum washing amount, the total flow of materials at two ends and the flow of the components in the total separation flow chart from top to bottom level by level, and the input and output total flows of the materials and the flow of the components in the input and output total flows of the connection level after the connection of outlets is adopted by adjacent separation units at the same level;
the stage number calculating module is used for calculating the stage number of an extraction stage and the stage number of a washing stage required by each separation unit;
the result output module is used for outputting a full separation flow chart with flow data and stage data and a percentage content change chart of each stage material in two phases according to the calculation results of the flow calculation module and the stage calculation module.
Some principles and concepts of the design system and the design method of the multi-component linkage extraction separation process according to the present invention are explained as follows.
(1) The sequence of extraction in a specific solvent extraction system is A from easy to difficult1、A2、…、AtThe extraction reaction between these components is in accordance with the exchange extraction mechanism, i.e. any two components AjAnd AiThe extraction reaction is carried out according to the following exchange reaction formula, and has the characteristic of constant mixed extraction ratio:
AjLz+Ai＝AiLz+Aj(1≤i<j≤t) (1)
wherein L is an extracting agent, and z is the number of components in the extract composition combined with the extracting agent.
(2) In FIG. 2, the separation units containing the same number of components in the feed liquid are arranged in the same separation layer stage, and the most difficult-to-extract components in the feed liquid are arranged from front to back in the flow chart according to the sequence from difficult-to-extract to easy-to-extract, such as the feed liquidWherein the separation units containing (t-2) components are positioned in the same separation level, and the front and back orders of the arrangement of the separation units are as follows: (A)tAt-1…A4)/(At-1At-2…A3)、(At-1At-2…A3)/(At-2At-3…A2)、 (At-2At-3…A2)/(At-3At-4…A1)。
The total separation flow chart of FIG. 2 has (t-1) levels, each level comprises separation units from top to bottom as 1, 2, … and (t-1), and the total separation units is (t-1)! And (4) respectively. Wherein each separation unit has the function of realizing one-time separation of feed liquid supplied to the separation unit in a countercurrent extraction mode, and the separation effect is as follows: the component flowing out of the aqueous phase outlet does not contain one of the most extractable components of the given feed solution, and the organic phase outlet does not contain one of the most difficult to extract components of the given feed solution.
For example, when the feed liquid used contains Ap、Ap+1、…、Aq(1≤p<q is less than or equal to t), the separation mode is always as follows: (A)qAq-1…Ap+1)/(Aq-1Aq-2…Ap) Wherein the part before "/" is the component flowing out from the aqueous phase outlet and contains Aq、Aq-1、…、Ap+1Containing only A in the feed liquidpComponent (A)pIs the most extractable component); the portion behind "/" flows out of the organic phase outlet and contains Aq-1、Aq-2、…ApContaining no A in the feed solutionqComponent (A)qThe most difficult component to extract). The material with one component reduced from the outlet at the two ends of one separation unit is provided for other separation units to continue extraction separation with the same effect as the feed liquid until the produced material only contains one component.
Each separation unit comprises two parts, namely an extraction section and a washing section, wherein the extraction sections of the two parts are n and m respectively, the 1 st stage of the extraction section extractor is an aqueous phase outlet, and the nth stage is connected with the 1 st stage of the washing section, so that the 1 st stage of the washing section is the total (n +1) th stage in the separation unit, and the last 1 stage of the washing section, namely the total (n + m) th stage of the separation unit, is an organic phase outlet.
When the number of the materials such as the contained components at the outlets at the two ends of each separation unit exceeds 1, the materials serving as the material liquid of other separation units are continuously separated until single components are separated. In the flow chart, the separation units with the same component number of the feed liquid are connected with each other to form a separation layer, wherein the front and back sequence of the connection arrangement of the separation units is the sequence from the difficultly extracted component to the easily extracted component contained in the feed liquid.
Any two adjacent separation units in the same level are connected in an outlet linkage mode, namely: the organic phase outlet of the former separating unit is connected with the aqueous phase outlet of the latter separating unit, so that the former separating unit provides an extracted organic phase for the latter separating unit, and the latter separating unit provides washing liquid for the former separating unit, thereby saving the consumption of chemical reagents which are originally needed. And (3) providing the multi-component material obtained after linkage connection for the next separation level, namely, taking the separation level with one less component number in the material liquid as the material liquid to continue to separate until the material obtained by separation only contains one component.
For two adjacent separation levels, the extracted organic phase or washing liquid required by any separation unit in the previous level is provided by the next level separation unit which uses the separation unit to provide feed liquid in a feeding-stage flowing mode.
The separation unit adopting the feeding-stage linkage mode is a separation unit which is used for receiving water phase/organic phase feed liquid, leading out an organic phase/water phase from the feeding stage and returning the organic phase/water phase to the previous stage for providing the feed liquid to the previous stage, and using the separation unit as an extraction organic phase/washing liquid so as to save the consumption of chemical reagents originally required by the previous stage separation unit. The process of simultaneously extracting the organic phase from the aqueous phase feed liquid is called aqueous phase feeding stage linkage, and the process of extracting the aqueous phase from the aqueous phase feed liquid is called organic phase feeding stage linkage.
(3) When water-phase feed liquid is used, the feed liquid enters the separation unit from an extractor connected with the washing section in the extraction section, namely the nth-stage extractor is a feeding stage; when organic phase feed liquid is used, the feed liquid enters from an extractor connected with the washing section and the extraction section, namely, the (n +1) th-stage extractor is a feeding stage; if two kinds of feed liquid of the water phase and the organic phase are used simultaneously, the feed liquid of the water phase enters the separation unit from the nth stage and the feed liquid of the organic phase enters the (n +1) th stage.
(4) The separation units can be divided into four types: 1 separation unit for separating initial feed liquid is marked as type I, and the feed stage is not linked with other separation units; the first separation unit at each level below is marked as type II, and the separation units are characterized in that a water phase feeding level linkage mode is adopted; the last separation unit of each level is marked as type III, and the method is characterized in that an organic phase feeding level linkage mode is adopted; all other separation units except the three types are marked as type IV, and the characteristic is that one of three conditions of water phase feeding stage linkage, organic phase feeding stage linkage or simultaneous receiving of two feed liquids of water phase and organic phase is possible to adopt.
The four types of separation units described above are further explained in connection with fig. 2.
The 1 separation unit for separating the initial feed liquid is marked as type I, and the characteristic is that the feeding stage is not linked with other separation units, namely (A) in figure 2tAt-1…A2)/(At-1At-2…A1) A separation unit.
The first separation unit in each stage below is designated as class II and is characterized by an aqueous feed cascade, as in FIG. 2 (A)tAt-1…A3)/(At-1At-2…A2) And (A)tAt-1…A4)/(At-1At-2…A3) Separation units which receive (A) separatelytAt-1…A2)/(At-1At-2…A1) And (A)tAt-1…A3)/(At-1At-2…A2) While separating the aqueous phase feed liquid of the unit, still draw an organic phase flow from the feed stage and return to the separation unit providing feed liquid for it and use as extracting the organic phase; in FIG. 2 (A)tAt-1…A2)/(At-1At-2…A1) And (A)tAt-1…A3)/(At-1At-2…A2) The arrows joining the separation units downwards indicate the flow direction of the feed liquid, and the arrows joining the separation units upwards indicate the direction of the return of the material drawn from the feed stage.
The last separation unit of each level is marked as type III, and the characteristic is that the linkage mode of organic phase feeding levels is adopted, as shown in (A) of figure 2t-1At-2…A2)/(At-2At-3…A1) And (A)t-2At-3…A2)/(At-3At-4…A1) Separation units which receive the signals from (A) respectivelytAt-1…A2)/(At-1At-2…A1) And (A)t-1At-2…A2)/(At-2At-3…A1) The organic phase of the separation unit is fed to a separation unit, which provides the organic phase with a feed liquid and also leads out an aqueous phase at the feed stage, which is returned to the separation unit for feeding the organic phase with the feed liquid, and the aqueous phase is used as a washing liquid.
All other separation units than the above three classes are designated as class IV, e.g. (A)t-1At-2…A3)/(At-2At-3…A2) A separation unit.
Any two adjacent separation units positioned at the same separation level are connected in an outlet linkage mode, namely an organic phase outlet positioned at the front separation unit is connected with a water phase outlet positioned at the rear separation unit, the former provides an extraction organic phase for the latter, and the latter provides a washing liquid for the former. As in FIG. 2 (A)tAt-1…A4)/(At-1At-2…A3) And (A)t- 1At-2…A3)/(At-2At-3…A2) Two separation units, the arrow to the right between them means that the former provides the extraction organic phase for the latter, the arrow to the left means that the latter provides the washing liquid for the former, and the arrow to the bottom is the surplus material after connection. If the surplus material only contains one component, the surplus material is taken as a product to be led out; if the component number is more than 1, the material is supplied to the IV type separation unit of the next separation layer stage as the materialThe liquid continues to separate. After the outlets of the two separation units are linked, the surplus materials can be a single water phase, a single organic phase or both, so that the IV type separation unit is characterized by being possible to adopt water phase feeding level linkage, organic phase feeding level linkage or simultaneously receive two kinds of feed liquid of the water phase and the organic phase.
A second object of the present invention is to provide a method for designing a system for performing a multi-component linkage extraction separation process as described above, so as to reduce the workload of determining and optimizing process parameters when designing a process for a rare earth linkage extraction separation process, and sufficiently and accurately determine the theoretical minimum extraction amount and the minimum washing amount.
To achieve the object, in a basic embodiment, the present invention provides a method for designing a system for performing a multi-component linkage extraction separation process, comprising the steps of:
(1) the data input module inputs the component number t to be separated and the component A to be separated1、 A2、…、AtCoefficient of separation between components to be separated
Figure BDA0001589519590000061
The requirements for impurities and calculation accuracy in the final product are met;
(2) the flow calculation module constructs a full separation flow chart according to the components to be separated and the number of the components, which are input by the data input module, and calculates the minimum extraction amount, the minimum washing amount, the total material flow of outlets at two ends and the component flow of each component in the full separation flow chart from top to bottom level by level, and the input and output material total flow and the component flow of each component in the input and output material total flow of a connection level after the outlets of adjacent separation units at the same level are linked;
(3) calculating the extraction stage number and the washing stage number required by each separation unit by the stage number calculating module;
(4) the result output module outputs a full separation flow chart with flow data and stage data and a percentage content change chart of components contained in the materials of each stage in two phases according to the calculation results of the flow calculation module and the stage calculation module;
(5) and summarizing and determining the minimum extraction amount and the minimum washing amount of the multi-component linkage extraction separation process according to the calculation result of the lowest separation level, namely the separation level containing 2 components in the used feed liquid.
In a preferred embodiment, the present invention provides a method for designing a system for multi-component coupled extraction separation process as described above, wherein the separation coefficient between the components to be separated is
Figure BDA0001589519590000071
For any two components AiAnd Aj(1≤i<j ≦ t) separation coefficient
Figure BDA0001589519590000072
Calculated from the following formula:
Figure BDA0001589519590000073
wherein i is more than or equal to 1 and j is less than or equal to t.
In a preferred embodiment, the present invention provides a method for designing a system for performing a multi-component coupled extraction separation process as described above, wherein in step (2),
for the type I separation unit, when the used feed liquid is a water phase, the calculation formulas of the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets at two ends and the flow of each component in the total flow are respectively as follows:
Figure BDA0001589519590000074
Figure BDA0001589519590000075
Figure BDA0001589519590000076
Figure BDA0001589519590000077
wherein i is more than or equal to 1 and less than or equal to t, and:
Sminminimum extract;
Wminis the minimum wash load;
Figure BDA0001589519590000078
is A1And AtThe separation factor between the two components;
Figure BDA0001589519590000079
is AiAnd AtThe separation factor between the two components;
Figure BDA00015895195900000710
is AiThe flow rate of the components in the aqueous phase feed liquid is
Figure BDA00015895195900000711
Figure BDA00015895195900000712
And
Figure BDA00015895195900000713
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure BDA00015895195900000714
and
Figure BDA00015895195900000715
respectively flowing out of the 1 st stage before linkage connectionThe total flow of all components in the phase and the total flow of all components in the organic phase flowing out of the n + m th stage (the units of the extraction amount, the washing amount and the flow of all materials are mol/unit time, the same applies below);
for the type I separation unit, when the used feed liquid is an organic phase, the calculation formulas of the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets at two ends and the flow of each component in the total flow are respectively as follows:
Figure BDA0001589519590000081
Figure BDA0001589519590000082
Figure BDA0001589519590000083
Figure BDA0001589519590000084
wherein i is more than or equal to 1 and less than or equal to t, and:
Sminminimum extract;
Wminis the minimum wash load;
Figure BDA0001589519590000085
is A1And AtThe separation factor between the two components;
Figure BDA0001589519590000086
is A1And AiThe separation factor between the two components;
Figure BDA0001589519590000087
is AiFlow rate of the components in the organic phase feed liquid, and
Figure BDA0001589519590000088
Figure BDA0001589519590000089
and
Figure BDA00015895195900000810
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure BDA00015895195900000811
and
Figure BDA00015895195900000812
respectively the total flow of all components in the water phase flowing out of the 1 st level and the total flow of all components in the organic phase flowing out of the n + m level before linkage connection,
for the type I separation unit, when the used feed liquid is two feed liquids of a water phase and an organic phase, the calculation formulas of the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets at two ends and the flow of each component in the total flow are respectively as follows:
Figure BDA0001589519590000091
Figure BDA0001589519590000092
Figure BDA0001589519590000093
Figure BDA0001589519590000094
wherein i is more than or equal to 1 and less than or equal to t, and:
Sminminimum extract;
Wminis the minimum wash load;
Figure BDA0001589519590000095
is A1And AtThe separation factor between the two components;
Figure BDA0001589519590000096
is A1And AiThe separation factor between the two components;
Figure BDA0001589519590000097
is AiAnd AtThe separation factor between the two components;
Figure BDA0001589519590000098
is AiThe flow rate of the components in the aqueous phase feed liquid;
Figure BDA0001589519590000099
is AiThe flow rate of the components in the organic phase feed liquid;
Figure BDA00015895195900000910
and
Figure BDA00015895195900000911
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure BDA00015895195900000912
and
Figure BDA00015895195900000913
respectively before linked and flowing outThe total flow of all components in the aqueous phase from stage 1 and the total flow of all components out of the organic phase from stage n + m.
For the II-type separation unit, the minimum extraction amount, the minimum washing amount, the total flow of the materials at the two ends and the flow of the components in the materials are respectively calculated by the following formulas:
Figure BDA00015895195900000914
Figure BDA0001589519590000101
Figure BDA0001589519590000102
Figure BDA0001589519590000103
wherein p is not less than i not more than q and:
Sminminimum extract;
Wminis the minimum wash load;
Apand AqRespectively the components with the minimum number and the maximum number in the material liquid of the separation unit;
Figure BDA0001589519590000104
is ApAnd AqThe separation factor between the two components;
Figure BDA0001589519590000105
is ApAnd AiThe separation factor between the two components;
Figure BDA0001589519590000106
is AiAnd AqDivide between two componentsThe coefficient of separation;
Figure BDA0001589519590000107
is AiThe flow rate of the components in the aqueous phase feed liquid;
Figure BDA0001589519590000108
and
Figure BDA0001589519590000109
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure BDA00015895195900001010
and
Figure BDA00015895195900001011
the total flow of all components in the water phase flowing out of the 1 st level and the total flow of all components in the organic phase flowing out of the n + m level are respectively obtained before linkage;
yAiorganic phase A providing feed liquid separation units for extraction from the feed stage to the upper stagesiThe split flow of the components;
ysumthe sum of the flow rates of all components in the organic phase which provides the feed liquid separation unit for extraction from the feed stage to the upper stages and having:
ysum＝(Smin)H (27)
wherein (S)min)HTo provide the minimum extraction capacity required by the high level separation unit of the feed solution;
for the type III separation unit, the minimum extraction amount, the minimum washing amount, the total flow of the materials at the two ends and the flow of the components in the materials are respectively calculated by the following formulas:
Figure BDA0001589519590000111
Figure BDA0001589519590000112
Figure BDA0001589519590000113
Figure BDA0001589519590000114
wherein p is not less than i not more than q and:
Sminminimum extract;
Wminis the minimum wash load;
Apand AqRespectively the components with the minimum number and the maximum number in the feed liquid of the separation unit;
Figure BDA0001589519590000115
is ApAnd AqThe separation factor between the two components;
Figure BDA0001589519590000116
is ApAnd AiThe separation factor between the two components;
Figure BDA0001589519590000117
is AiAnd AqThe separation factor between the two components;
Figure BDA0001589519590000118
is AiThe flow rate of the components in the organic phase feed liquid;
Figure BDA0001589519590000119
and
Figure BDA00015895195900001110
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure BDA0001589519590000121
and
Figure BDA0001589519590000122
the total flow of all components in the water phase flowing out of the 1 st level and the total flow of all components in the organic phase flowing out of the n + m level are respectively obtained before linkage;
p is not less than i and not more than q is ApAnd AqRespectively the components with the minimum number and the maximum number in the feed liquid of the separation unit;
Figure BDA0001589519590000123
providing A in the aqueous phase flow of the feed liquid separation unit for extraction from the feed stage to the high-stageiThe flow rates of the components to be separated,
xsumproviding the sum of the flow rates of all components in the aqueous phase stream of the feed liquid separation unit for extraction from the feed stage to the upper stage, and having:
xsum＝(Wmin)H (34)
wherein (W)min)HTo provide the minimum amount of washing required by the high level separation unit of the feed solution.
In a more preferred embodiment, the present invention provides a method for designing a system to perform a multi-component linkage extraction separation process, wherein in step (2), for two adjacent separation units located at the same level, the organic phase outlet of the previous separation unit L is connected with the aqueous phase outlet of the next separation unit R, the separation unit L provides an organic phase for extraction for the separation unit R, and simultaneously, the separation unit R provides a washing liquid for the separation unit L, the total input and output material flow rates and the component flow rates of the subsequent connection stage are connected, and the total material flow rate and the component flow rate of the subsequent connection stage are connected and output to the next separation stage as follows:
1) first, compare
Figure BDA0001589519590000124
And
Figure BDA0001589519590000125
and (W)min)LA size of between, wherein
Figure BDA0001589519590000126
And (W)min)LRespectively representing the total flow of each component of the organic phase outlet and the required minimum washing amount before the linkage of the previous separation unit,
Figure BDA0001589519590000127
and (S)min)RRespectively representing the total flow of all components of the water phase outlet and the required minimum extraction amount before linkage of the next separation unit;
2) the following three cases may occur as a result of the comparison:
Figure BDA0001589519590000128
Figure BDA0001589519590000129
Figure BDA0001589519590000131
3) in the first case, when both (35) and (36) are simultaneously established, the organic phase outlet flow (y) of the separation unit L is linked and connectedsum,n+m)LCalculated as follows:
Figure BDA0001589519590000132
linked connected aqueous phase outlet flow (x) of the rear separation unit Rsum,1)RCalculated by the following formula：
Figure BDA0001589519590000133
In this case, after linkage connection, if the net output organic phase contains only 1 component, that is, it is extracted as the product, and if the component contains more than 1 component, the next-stage phase-connected IV type separation unit is provided as the feed liquid, and the total flow rate f of the feed liquidoCalculated as follows:
Figure BDA0001589519590000134
wherein the split flow of each component
Figure BDA0001589519590000135
Calculated as follows:
Figure BDA0001589519590000136
wherein,
Figure BDA0001589519590000137
the split flow of each component in the organic phase outlet before the previous separation unit is linked,
Figure BDA0001589519590000138
the rear separation unit is linked with the split flow of each component in the front water phase outlet;
4) in the second case, when both (37) and (38) are simultaneously established, the outlet flow (y) of the organic phase of the separation unit L is linked and connectedsum,n+m)LCalculated as follows:
Figure BDA0001589519590000139
linked connected aqueous phase outlet flow (x) of the rear separation unit Rsum,1)RCalculated as follows:
Figure BDA00015895195900001310
after linkage connection, if the water phase produced in net contains only 1 component, namely the water phase is taken out as a product, if the component contained in the water phase exceeds 1 component, the material liquid of the IV type separation unit connected with the next layer is provided as a single water phase, and the total flow rate f of the material liquidaCalculated as follows:
Figure BDA0001589519590000141
wherein the split flow of each component
Figure BDA0001589519590000142
Calculated as follows:
Figure BDA0001589519590000143
wherein,
Figure BDA0001589519590000144
the split flow of each component in the organic phase outlet before the previous separation unit is linked,
Figure BDA0001589519590000145
the rear separation unit is linked with the split flow of each component in the front water phase outlet;
5) the third situation is that when the two types (39) and (40) are simultaneously established, the organic phase outlet flow (y) of the separation unit L is linked and connectedsum,n+m)LCalculated as follows:
Figure BDA0001589519590000146
linked connected aqueous phase outlet flow (x) of the rear separation unit Rsum,1)RCalculated as follows:
Figure BDA0001589519590000147
after linkage connection, if the net produced water phase and organic phase only contain 1 component, namely the net produced water phase and organic phase are taken out as products, if the net produced components contain more than 1 component, the water phase and organic phase feed liquid is simultaneously provided for the IV type separation unit connected with the next layer, and the total flow f of the water phase and the organic phase feed liquid is respectivelyaAnd foThe calculation is carried out according to the following two formulas:
Figure BDA0001589519590000148
Figure BDA0001589519590000149
wherein the flow rate of each component in the two-phase feed liquid is divided
Figure BDA00015895195900001410
And
Figure BDA00015895195900001411
the calculation is carried out according to the following two formulas:
Figure BDA00015895195900001412
Figure BDA00015895195900001413
wherein,
Figure BDA00015895195900001414
the split flow of each component in the organic phase outlet before the previous separation unit is linked,
Figure BDA00015895195900001415
the rear separation unit is linked with the split flow of each component in the front water phase outlet.
In a more preferred embodiment, the present invention provides a method for designing a system to perform a multi-component linkage extraction separation process, wherein in step (2), for the type IV separation unit, the used feed liquid is derived from the material that is net produced after the outlets of two adjacent separation units in the previous separation stage are linked, and the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets of the two ends and the respective component flow rates thereof required for separation are calculated as follows:
1) when the feed liquid provided by the previous separation level is a water phase, calculating according to the formulas (21) to (27) by adopting a water phase feeding level linkage mode;
2) when the feed liquid provided by the previous separation level is an organic phase, calculating according to the formulas (28) to (34) by adopting an organic phase feeding level linkage mode;
3) when the feed liquid provided by the previous separation level is two feed liquids of a water phase and an organic phase, calculating according to the following formula;
Figure BDA0001589519590000151
Figure BDA0001589519590000152
Figure BDA0001589519590000153
Figure BDA0001589519590000154
wherein p is not less than i not more than q and:
Apand AqRespectively the components with the minimum number and the maximum number in the feed liquid of the separation unit;
Sminminimum extract;
Wminis the minimum wash load;
Figure BDA0001589519590000155
is ApAnd AqThe separation factor between the two components;
Figure BDA0001589519590000161
is ApAnd AiThe separation factor between the two components;
Figure BDA0001589519590000162
is AiAnd AqThe separation factor between the two components;
Figure BDA0001589519590000163
is AiThe flow rate of the components in the aqueous phase feed liquid;
Figure BDA0001589519590000164
is AiThe flow rate of the components in the organic phase feed liquid;
Figure BDA0001589519590000165
and
Figure BDA0001589519590000166
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure BDA0001589519590000167
and
Figure BDA0001589519590000168
the total flow of all components flowing out of the water phase of the 1 st stage and the total flow of all components flowing out of the organic phase of the n + m th stage before linkage connection are respectively.
In a more preferred embodiment, the present invention provides a method for designing a system to perform a multi-component linkage extraction separation process, wherein in step (2), when calculating total input and output material flow rates of a connection stage after linkage of outlets of two adjacent separation units at the front and back of the same level and flow rates of each component therein, if the number of components contained in the material liquid of the level is 2, that is, the separation unit is located at the lowest separation level, and both of (35) and (36) are satisfied, then a blank washing liquid needs to be supplemented to the separation unit L, and the flow rate of the supplemented blank washing liquid is calculated according to the following formula:
Figure BDA0001589519590000169
wherein,
(Wadd)La newly added flow of blank wash liquid for the separation unit L;
(Wmin)Lrepresents the minimum amount of washing required for the separation unit L;
Figure BDA00015895195900001610
and (S)min)RRespectively representing the total flow of all components of the water phase outlet and the required minimum extraction amount before the linkage of the separation unit R;
in a more preferred embodiment, the present invention provides a method for designing a system to perform a multi-component linkage extraction separation process, wherein in step (2), when calculating total input and output material flow rates of a connecting stage and component flow rates of each component in the input and output material flow rates after linkage of outlets of two adjacent separation units in front of and behind the same level, if the component number in the feed liquid of the level is 2, that is, the separation unit is already located at the lowest separation level, and both the formulas (37) and (38) are satisfied, then a blank extraction organic phase needs to be supplemented to the separation unit R, and the flow rate of the supplemented blank extraction organic phase is calculated according to the following formula:
Figure BDA00015895195900001611
wherein,
(Sadd)Rextracting the organic phase flow for the newly added blank of the separation unit R;
(Smin)Rrepresents the minimum extraction required for the separation unit R;
Figure BDA0001589519590000171
and (W)min)LRespectively representing the total flow of all components of the organic phase outlet and the required minimum washing amount before the linkage of the separation unit L;
in a more preferred embodiment, the present invention provides a method for designing a system for performing a multi-component linkage extraction separation process as described above, wherein in step (5), the total minimum extraction amount and the total minimum washing amount required for the whole separation process are determined in a summary manner according to the calculation results of the separation levels of 2 components in the feed liquid used, and the method comprises:
the total minimum extraction amount is equal to the sum of the minimum extraction amount of the type II separation unit at the lowest level and the flow of the blank extraction organic phase which needs to be supplemented after the outlets of all adjacent separation units at the lowest level are linked;
the total minimum washing amount is equal to the sum of the minimum washing amount of the type III separation unit at the lowest level and the flow of the blank washing liquid which needs to be supplemented after the outlets of all the adjacent separation units at the lowest level are linked and connected.
The invention has the advantages that the multi-component linkage extraction separation process design system and the design method can reduce the workload of determining and optimizing process parameters when being used for the process design of the rare earth linkage extraction separation process, and can fully and accurately judge the theoretical minimum extraction amount and the minimum washing amount according to the principle.
In the field of solvent extraction separations, the theoretical lower limits for the minimum extraction and minimum wash capacity required for full separation of multiple components are lacking in both basic theory and computational methods. The invention provides a calculation formula and a software system for designing the multi-component extraction total separation process with theoretical minimum extraction amount and minimum washing amount, and can simultaneously define the limit target which can be reached for the design of the multi-component solvent extraction separation process flow, improve the efficiency of the flow design work and avoid the blindness in the design process.
Drawings
FIG. 1 is a block diagram of an exemplary multi-component coupled extraction separation process design system of the present invention.
FIG. 2 is a framework diagram of a full separation process constructed by a flow calculation module according to data from a data input module in an exemplary multi-component linkage extraction separation process design system of the present invention.
FIG. 3 is a flow diagram of an exemplary multi-component coupled extraction separation process design method of the present invention.
Fig. 4 is a block diagram of a linkage extraction flow constructed by the multi-component linkage extraction separation flow design method of the present invention in example 1 of the specific embodiment.
Fig. 5 is a data diagram of linkage connection relationship and flow rate change of the separation units B and C in example 1 according to the specific embodiment.
Fig. 6 is a diagram of an output result of the result output module of example 1 in a specific embodiment.
FIG. 7 is a graph of the percentage change of the components of two separate levels in two phases, as output from example 1 of the preferred embodiment, wherein the upper graph is the first level and the lower graph is the second level.
Fig. 8 is a block diagram of a linkage extraction flow constructed by the multi-component linkage extraction separation flow design method according to the present invention in example 2 of the embodiment.
Fig. 9 is a data diagram of linkage connection relationship and flow rate change of the separation units B and C in example 2 according to the specific embodiment.
Fig. 10 is a data diagram of linkage connection relationship and flow rate change of the separation units D and E in example 2 according to the embodiment.
Fig. 11 is a data diagram of linkage connection relationship and flow rate change of the separation units E and F in example 2 according to the embodiment.
Fig. 12 is a diagram of an output result of the result output module of example 2 in the detailed embodiment.
Detailed Description
An exemplary multi-component linkage extraction separation process design system of the present invention is shown in fig. 1, and includes four parts, a data input module, a flow calculation module, a stage calculation module, and a result output module.
An exemplary operating flow of the multi-component linkage extraction separation flow design method of the present invention is shown in fig. 3, and includes the following steps:
(1) the flow calculation module constructs a full separation flow frame diagram as shown in FIG. 2 according to the data of the data input module;
(2) calculating the split flow, the total flow and the required minimum extraction amount and minimum washing amount of each component in the outlets at two ends of the first layer of fraction separation unit in the total separation flow chart according to the formulas (3) - (8), (9) - (14) or (15) - (20) respectively according to the condition that the feed liquid is an aqueous phase and an organic phase or the aqueous phase and the organic phase are two phases;
(3) calculating the split flow, total flow and the minimum extraction amount and minimum washing amount of each component in outlets at two ends of a front separation unit and a rear separation unit of a second level of the separation unit according to formulas (21) - (27) and (28) - (34) by the first-level calculation data respectively;
(4) then, calculating the linkage connection of the outlets between the two separated units at the second level according to the methods of the formulas (35) to (56);
(5) if the third separation level exists, calculating the divided flow rate, the total flow rate and the required minimum extraction amount and minimum washing amount of each component in the outlets at two ends of the II-type separation unit and the III-type separation unit in the third level according to the formulas (21) to (27) and (28) to (34) respectively according to the calculation data of the second level;
(6) calculating the optimized flow rate of the third-level IV separation unit according to the formulas (21) - (27), (28) - (34) or (55) - (60) respectively according to three different conditions that the feed liquid provided to the third-level IV separation unit is an aqueous phase, an organic phase or a two-phase after the outlets of the second-level two separation units are linked and connected;
(7) if more levels exist, sequentially calculating the optimized flow of each separation unit and linkage connection between adjacent separation units of each level downwards layer by layer according to the same calculation method of the third level;
(8) the calculation result of the flow calculation module is provided for a series calculation module, the series of the extractors of the extraction section and the washing section required for all the separation units to reach the separation requirement in the flow frame diagram is calculated through static simulation, and the percentage content value of all the components in each separation unit in two phases is changed along with the series;
(9) and finally, providing the calculation data of the flow calculation module and the series calculation module for a result output module, and outputting a full separation flow chart containing flow and series data and a percentage content chart of all components of each separation layer level in two phases along with the change of the series through a system interface.
The following examples further illustrate embodiments of the present invention.
Example 1
For a GdCl-containing3、EuCl3And SmCl3Three aqueous phase feed liquids of the components to be separated, wherein the separation aims to obtain SmCl with the purity of 99.99 percent3、EuCl3And GdCl3Three kinds of products. P507-kerosene is adopted as an extraction organic phase, alkali is consumed for saponification of the extraction organic phase in the separation process, and acid is consumed in the washing process of the washing section. The invention can quickly design and obtain an extraction full separation process with the theoretical minimum consumption of acid and alkali, namely the designed full separation process has the theoretical minimum extraction amount and the minimum washing amount.
Inputting Gd, Eu and Sm to be separated into components by a data input module; gd. Flow rate f of Eu and Sm in feed liquidGd,a、fEu,a、fSm,aRespectively input at 0.3000, 0.1000 and 0.6000, and the total flow rate faIs 1.0000; Eu/Sm separation coefficient betaEu/SmIs 2.34, Gd/Eu separation coefficient betaGd/EuIs 1.50; the impurity requirement of the product is 1e-4, and the calculation precision of the series is 1 e-4. And clicking the RUN button to finish flow calculation and stage number calculation, and automatically outputting a flow chart and a percentage content chart of each stage of component. The operational calculation process is detailed below.
The procedure begins with designing a flow diagram frame as shown in fig. 4, comprising three separation units (SmEu)/(EuGd), Sm/Eu, Eu/Gd, designated as separation units A, B and C, respectively.
Gd in all feed liquid of the separation unit A flows out from the organic phase outlet, Sm flows out from the aqueous phase outlet, so that the flow of the Sm component in the aqueous phase outlet of the separation unit A before linkage
Figure BDA0001589519590000201
And the flux of Gd component in the outlet of the organic phase
Figure BDA0001589519590000202
Respectively as follows:
Figure BDA0001589519590000203
flow rate of aqueous phase of intermediate component Eu at outlets at two ends of separation unit A
Figure BDA0001589519590000204
And organic phase flow
Figure BDA0001589519590000205
Calculated from equations (5) and (6), respectively, as follows:
Figure BDA0001589519590000206
then, the minimum extraction amount (S) required by the separation unit A is calculated by the formulas (3) and (4) respectivelymin)AAnd minimum washing amount (W)min)ARespectively as follows:
Figure BDA0001589519590000207
separation unit B was then calculated. The separation unit B belongs to a II-type separation unit, and adopts a water phase feeding level linkage mode to lead out an organic phase flow and keep the extraction balance with the provided water phase feed liquid, so that the flow (y) of two components of Sm and Eu in the separation unit BSm)BAnd (y)Eu)BCan be solved by the following equation system:
Figure BDA0001589519590000208
the solution may have:
Figure BDA0001589519590000209
thus, the amount of the Sm and Eu split in the feed solution of separation Unit B (f)Sm,a)BAnd (f)Eu,a)BRespectively as follows:
Figure BDA00015895195900002010
wherein (x)Sm,1)AAnd (x)Eu,1)AThe flow rates of the components Sm and Eu at the water phase outlet of the separation unit A after linkage connection with the separation unit B are respectively. Further, the minimum extraction amount (S) of the Sm/Eu separation unit can be calculated from equations (21) and (22), respectivelymin)BAnd minimum washing amount (W)min)BRespectively as follows:
Figure BDA0001589519590000211
(fa)Bthe total flow rate of the feed liquid for separating components Sm and Eu of the unit B. All Sm components which are net to flow into the separation unit B flow out from the water phase outlet, all Eu components flow out from the organic phase outlet, and therefore the flow of the Sm components in the water phase outlet of the front separation unit B is linked
Figure BDA0001589519590000212
And the flow rate of the Eu component in the organic phase outlet
Figure BDA0001589519590000213
Respectively as follows:
Figure BDA0001589519590000214
the flow rate of the pure Sm component in the product from the separation unit B is 0.6000, which is the same as the flow rate of the pure Sm component in the feed liquid, namely, all the Sm component in the original feed liquid flows out from the water phase outlet of the separation unit B.
The separation unit C is calculated next. The separation unit C belongs to a III-class separation unit, and adopts an organic phase feeding level linkage mode to lead out an aqueous phase flow to be in extraction balance with the provided organic phase feed liquid, so that the flow (x) of Eu and Gd in the aqueous phase flow is balanced with the flow of the provided organic phase feed liquidEu)CAnd (x)Gd)CThe following equation can be solved:
Figure BDA0001589519590000215
the solution is as follows:
Figure BDA0001589519590000216
thus, the split flow (f) of the two Eu and Gd components in the feed liquid of separation unit CEu,o)CAnd (f)Gd,o)CRespectively as follows:
Figure BDA0001589519590000217
the minimum extraction amount (S) of the Eu/Gd separation unit can be further calculated from equations (28) and (29)min)CAnd minimum washing amount (W)min)CRespectively as follows:
Figure BDA0001589519590000218
wherein (f)o)CThe total flow of feed solution for separating the C components Eu and Gd of the unit. All the Eu component which flows into the separation unit C cleanly flows out from the water phase outlet, all the Gd component flows out from the organic phase outlet,thereby linking the flow rate of the Eu component in the aqueous phase outlet of the preceding separation Unit C
Figure BDA0001589519590000221
And the flux of Gd component in the organic phase outlet
Figure BDA0001589519590000222
Respectively as follows:
Figure BDA0001589519590000223
at this time, the flow rate of the pure Gd component flowing out of the separation unit C is 0.3000, which is the same as the flow rate of Gd component in the feed liquid, i.e. all Gd components in the original feed liquid flow out of the organic phase outlet of the separation unit C.
And analyzing the condition of the separation unit B and the separation unit C after the exit linkage connection. Analysis in this example is readily known:
Figure BDA0001589519590000224
wherein,
Figure BDA0001589519590000225
and
Figure BDA0001589519590000226
the flow rate of the Eu component in the organic phase outlet of the separation unit B and the flow rate of the water phase outlet of the separation unit C before linkage connection are respectively adopted, so that only one Eu component exists, and the Eu flow rate is the total flow rate; (W)min)BAnd (S)min)CThe minimum wash capacity of separation unit B and the minimum extract capacity of separation unit C, respectively. Thus, separation unit C needs to be replenished with a blank extractant, and the blank extractant flow (S) needs to be replenishedadd)CCalculated according to equation (62) as:
(Sadd)C＝0.2783
the flow rate changes before and after linkage and connection of the separation units B and C are shown in FIG. 5. Before linkage connectionFlow rate of Eu component at organic phase outlet of separation unit B
Figure BDA0001589519590000227
0.0466, the minimum amount of washing (W) required to separate Unit B is shown by the comparison abovemin)BCan be provided entirely by linkage connection, so that after linkage connection, the Eu component flow (y) of the organic phase outlet of the separation unit B isEu,n+m)BCalculated according to equation (45) as 0.0466+0.1133 ═ 0.1599, minimum extraction (S) required to isolate unit Cmin)C0.4382, and the organic phase supplied by separation unit B is only 0.1599, so that separation unit C needs to be supplemented with a flow rate (S) of the air-white extracted organic phaseadd)CComprises the following steps: 0.4382-0.1599 is 0.2783, but since the flow rate of Eu component is only 0.1599, the flow rate of water phase outlet of separation unit C is linked (x)Eu,1)CCalculated according to equation (46) as: 0.0534+0.0466+0.1133 ═ 0.2113, and the aqueous phase, minus the flow rate 0.1133, satisfied separation unit B its minimum wash capacity (W)min)BIn addition, the residual water phase with the residual flow rate of 0.1000 part is the Eu product, namely the water phase flow rate p of the Eu productEu,aThe Eu concentration is 0.1000, namely, all Eu in the original feed liquid is obtained to obtain a water-phase product.
Then, the static simulation of each separation unit is carried out by a series calculation module. Take separation unit a as an example. The material balance and the extraction balance of the 1 st stage water phase outlet can be known as follows:
Figure BDA0001589519590000231
wherein (x)Gd,1)A、(xEu,1)AAnd (x)Sm,1)ARespectively, the water phase flow of Gd, Eu and Sm components flowing out of the 1 st stage, (y)Gd,1)A、(yEu,1)AAnd (y)Sm,1)ARespectively the flow rates of Gd, Eu and Sm component organic phases flowing out of the 1 st level. The separation coefficient is an input value, (S)min)A、(xEu,1)AAnd (x)Sm,1)ACalculated to obtain (x)Gd,1)AThe value is set to (x) according to the separation requirementEu,1)A×10-4，(yGd,1)A、(yEu,1)AAnd (y)Sm,1)AFor the unknowns, the solution knows:
Figure BDA0001589519590000232
then, the material transfer balance relationship of each component of the 1 st stage and the 2 nd stage is known as follows:
Figure BDA0001589519590000233
Figure BDA0001589519590000234
the component flow rates of Sm, Eu and Gd components at the water phase outlets of the separation unit A before linkage connection are respectively. The flow of the organic phase (y) out of the components of the extractor of stage 2 can then be determined from the feed and extraction balances of the extractor of stage 2 in the same manner as described aboveGd,2)A、 (yEu,2)AAnd (y)Sm,2)AThen the flow rate (x) of each component water phase flowing out of the extractor of the 3 rd stage is obtained by the material transfer balance between the 2 nd stage and the 3 rd stageGd,3)A、(xEu,3)AAnd (x)Sm,3)AAnd performing recursion calculation step by step until the relative change of the flow of the water phase of the same component of two adjacent stages is smaller than the set calculation accuracy 1e-4, and performing recursion calculation for 62 times in the extraction section of the separation unit A at the moment, namely, the stage number n required by the extraction section of the separation unit A is 62. The washing section of the separation unit a is calculated from the last stage, i.e. the (n + m) th stage, in the same way as the extraction section, the number of recursion calculations is 36, the number of stages m required by the washing section of the separation unit a is 36, and the two stages together need 98 stages. The same calculation shows that the number of extractor stages required for separation units B and C is 77 and 174, respectively. Thus, the total number of extractor stages required for the total separation scheme is: stage 349 is 98+77+ 174.
Finally, the system gives a full separation flow chart of flow data and series data according to the calculation result, such as a graph in FIG. 6, and a graph in which the percentage change of each component in two phases of two levels is shown in FIG. 7. In fig. 6, the minimum extraction capacity of the separation unit B is 0.9117, but after the separation units B and C are linked, the extraction organic phase with the extraction capacity of 0.2783 needs to be supplemented at the linkage joint, so that the theoretical minimum extraction capacity required by the total flow is the sum of the two, which is 1.1900; the minimum washing amount of the separation unit C is 0.8900, and the separation unit B does not need to be supplemented with washing liquid, so the total minimum washing amount of the process is 0.8900. Through the extraction separation of the designed process, the purity of the finally obtained product is 99.99 percent, the Sm and Eu products are water phase, and the Gd product is organic phase.
Example 2
The feed liquid to be separated contains NdCl3、PrCl3、CeCl3And LaCl3Four aqueous phases of the components to be separated, with the aim of obtaining LaCl with a purity of 99.99%3、CeCl3、PrCl3And NdCl3Four products. P507-kerosene is adopted as an extraction organic phase, alkali is consumed for saponification of the extraction organic phase in the separation process, and acid is consumed in the washing process. The invention can quickly design and obtain an extraction full separation process with the minimum consumption of acid and alkali theories.
Inputting components to be separated into Nd, Pr, Ce and La in a data input module; their flow rate f in the feed liquidNd,a、fPr,a、fCe,a、fLa,aRespectively input at 0.1500, 0.0500, 0.5000 and 0.3000, total flow rate faIs 1.0000; separation coefficient beta of Ce/La, Pr/Ce and Nd/PrCe/La、βPr/CeAnd betaNd/PrInputs were 6.83, 2.03 and 1.55, respectively; the impurity requirement of the product is 1e-4, and the calculation accuracy of the series is 1 e-4. And clicking the RUN button to finish flow calculation and progression calculation, and automatically outputting a flow chart and a percentage content chart of each hierarchy component.
The procedure first designed a flow diagram frame as shown in FIG. 8, comprising six separation units (LaCePr)/(CePrNd), (LaCe)/(CePr), (CePr)/(PrNd), La/Ce, Ce/Pr, Pr/Nd, respectivelySeparation unit A, B, C, D, E, F. The flow calculation of the three separation units of the separation unit A, B, C and the linkage connection calculation of the two separation units B and C are the same as those in embodiment 1, and are not described herein again. In contrast, after B and C are linked, the possible shortage of the extraction organic phase or the washing liquid can be provided by the lower-stage Ce/Pr separation unit in a feeding cascade mode without supplementing a blank extraction organic phase or washing liquid. The actual calculation result of linkage connection of the separation units B and C is shown in FIG. 9, where the separation unit C needs to supplement the flow of the extracted organic phase (S)add)C0.0638, separating element E needs to adopt water phase feeding stage linkage mode, before linkage, total flow of each component of feed liquid
Figure BDA0001589519590000251
Is 0.2117. The flow rate calculation and linkage connection of the separation unit D, E, F are described below.
The separation unit D belongs to a II-type separation unit, and is used for performing La/Ce separation of water phase feed level linkage, wherein the initial feed liquid is the flow of a water phase outlet of the separation unit B, and the flow of components Ce and La at the water phase outlet of the separation unit B before linkage
Figure BDA0001589519590000252
And
Figure BDA0001589519590000253
the calculation in the early stage respectively comprises:
Figure BDA0001589519590000254
organic phase flow (y) from the feed stage of the separation unit Dsum)DThe minimum extraction requirement of the separation unit B is just to be met, namely:
(ysum)D＝(Smin)B＝0.4476
because the organic phase flow led out from the feeding stage and the aqueous phase feed liquid actually entering the trough body are in an extraction balance state, the flow splitting (y) of Ce and La in the organic phase is led outCe)DAnd (y)La)DThe following equation can be used:
Figure BDA0001589519590000255
solving to obtain:
Figure BDA0001589519590000256
the Ce, La feed flow entering the feed stage of separation unit D at this point (f)Ce,a)DAnd (f)La,a)DRespectively as follows:
Figure BDA0001589519590000257
the minimum extraction amount and the minimum washing amount required for the separation unit D are calculated from equations (21) and (22), respectively, as follows:
Figure BDA0001589519590000258
(fa)Dthe total flow of feed solution for separating components Ce and La of unit D. All La components in the feed liquid flowing into the separation unit D flow out from the water phase outlet, all Ce components flow out from the organic phase outlet, and therefore the La components flow out from the water phase outlet of the separation unit D before linkage
Figure BDA0001589519590000261
And the Ce component flow at the outlet of the organic phase
Figure BDA0001589519590000262
Respectively as follows:
Figure BDA0001589519590000263
at the moment, the pure La product is obtained at the water phase outlet, and the flow rate is equal to the flow rate of the La component in the initial feed liquid.
The separation unit E is then analyzed. The separation unit E performs the linked Ce/Pr separation of the water phase and the feeding stage, and the flow rate (y) of the organic phase led out from the feeding stagesum)EIt is exactly equal to the fraction of the separation unit C with insufficient minimum extraction (S)add)CNamely:
(ysum)E＝(Sadd)C＝0.0638
net flow into separation unit E feed stages Ce and Pr
Figure BDA0001589519590000264
And
Figure BDA0001589519590000265
calculated by the upper layer, the following are respectively:
Figure BDA0001589519590000266
the organic phase flow led out from the feeding stage of the separation unit E and the aqueous phase feed liquid actually entering the trough body are in extraction balance, so that the following equation system is provided:
Figure BDA0001589519590000267
solving the obtained partial flow (y) of Pr and Ce components in the organic phase led out by the separation unit EPr)EAnd (y)Ce)E：
Figure BDA0001589519590000268
The two partial flows (f) in the aqueous feed liquid which now enters the feed stage of the separation unit EPr,a)EAnd (f)Ce,a)ERespectively as follows:
Figure BDA0001589519590000269
then, the minimum extraction amount and the minimum washing amount (S) required for the separation unit E are calculated from the equations (21) and (22), respectivelymin)EAnd (W)min)EComprises the following steps:
Figure BDA0001589519590000271
all Ce components which flow into the feed liquid of the separation unit E are discharged from the aqueous phase outlet, all Pr components flow out from the organic phase outlet, so the Ce component flow out of the aqueous phase outlet of the separation unit E before linkage
Figure BDA0001589519590000272
And organic phase outlet Pr component flow
Figure BDA0001589519590000273
Respectively as follows:
Figure BDA0001589519590000274
the last separation unit F is analyzed again. The separation unit F carries out organic phase feeding level linkage Pr/Nd separation, feed liquid is from an organic phase outlet of the separation unit C, and the net flow of Nd and Pr in the feed liquid flowing into the separation unit F
Figure BDA0001589519590000275
And
Figure BDA0001589519590000276
respectively as follows:
Figure BDA0001589519590000277
flow (x) of the aqueous phase from the feed stagesum)FJust meet the minimum washing quantity (W) of the separation unit Cmin)CThe requirements, namely:
(xsum)F＝(Wmin)C＝0.3372
solving the following system of equations:
Figure BDA0001589519590000278
the component flow (x) of Nd and Pr components in the water phase extracted by the separation unit F can be obtainedNd)FAnd (x)Pr)F：
Figure BDA0001589519590000279
The amount of Nd and Pr split in the organic phase feed solution entering the feed stage of separation unit F (F)Nd,o)FAnd (f)Pr,o)FRespectively as follows:
Figure BDA00015895195900002710
the minimum extract and minimum wash capacity of the separation unit F can be calculated from equations (28) and (29), respectively, as follows:
Figure BDA00015895195900002711
the water phase outlet of the separation unit F only contains Pr component, the organic phase outlet only contains Nd component, and the outlet flow rates at two ends are respectively as follows:
Figure BDA0001589519590000281
at the moment, the pure Nd product is obtained at the organic phase outlet, and the flow rate is completely the same as that of the Nd product in the initial feed liquid.
The same method as in example 1 was used to perform the interlocking engagement between the separation units D and E, E and F, and the interlocking engagement results are shown in fig. 10 and 11, respectively. In FIG. 10, separation units D and E are connected to satisfy the minimum wash capacity requirement of separation unit D and the minimum extract capacity requirement of separation unit E simultaneously to obtainProduct Ce aqueous phase flow rate pCe,a0.3569, organic phase flow rate pCe,o0.1431 in total, which was 0.5000 in total, and was the same as the Ce flow rate in the initial feed liquid. In FIG. 11, when separation units E and F are coupled, the minimum washing amount of separation unit E cannot be satisfied, and the amount of blank washing liquid (W) to be supplemented is not satisfiedadd)E0.0054, pure Pr product obtained as organic phase, flow pPr,oIs 0.0500, the same as in the initial feed.
Minimum extraction (S) of the lowest-order separation unit Dmin)D0.8395, since the minimum extraction amount is not enough after the separation units D, E, E and F are linked and connected, the minimum extraction amount of the separation unit D is 0.8395, which is the total minimum extraction amount of the process. The minimum washing amount of the separation unit F is 0.4910, and after the separation units E and F are connected, the connection part needs to be supplemented with 0.0054, so that the theoretical total minimum washing amount required by the process is the sum of the two, namely 0.4964.
Static simulation was carried out in the same manner as in example 1, and it was found that the number of extractor stages required for six separation units was calculated to be 111, 133, 91, 54, 114 and 142 in this order, and 645 stages in total. The percentage of each component in the three separation levels output by the system as a function of the number of stages is shown in FIG. 12. The purity of the final product obtained by the designed process is 99.99 percent, the La product is a single aqueous phase, the Ce product is a partial aqueous phase and a partial organic phase, and the Pr and Nd products are organic phases.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is intended to include such modifications and variations. The foregoing examples or embodiments are merely illustrative of the present invention, which may be embodied in other specific forms or in other specific forms without departing from the spirit or essential characteristics thereof. The described embodiments are, therefore, to be considered in all respects as illustrative and not restrictive. The scope of the invention should be indicated by the appended claims, and any changes that are equivalent to the intent and scope of the claims are intended to be included therein.

Claims (7)

1. A design method for carrying out multi-component linkage extraction separation process by utilizing a multi-component linkage extraction separation process design system,
the design system comprises a data input module, a flow calculation module, a progression calculation module and a result output module,
the data input module is used for inputting the component fraction t to be separated and the component A to be separated1、A2、…、AtCoefficient of separation between components to be separated
Figure FDA0003330892150000011
The requirements for impurities and calculation accuracy in the final product are met; wherein t is more than or equal to 3, i is more than or equal to 1 and less than or equal to t-1, and the components to be separated in the used extraction system are A according to the sequence of easy extraction and difficult extraction1、A2、…、At；
The flow calculation module is used for constructing a full separation flow chart according to the components to be separated and the number of the components to be separated, which are input by the data input module, and calculating the minimum extraction amount, the minimum washing amount, the total flow of materials at two ends and the flow of the components in the total separation flow chart from top to bottom level by level, and the input and output total flows of the materials and the flow of the components in the input and output total flows of the connection level after the connection of outlets is adopted by adjacent separation units at the same level;
the stage number calculating module is used for calculating the stage number of an extraction stage and the stage number of a washing stage required by each separation unit;
the result output module is used for outputting a full separation flow chart with flow data and stage data and a percentage content change chart of components contained in each stage material in two phases according to the calculation results of the flow calculation module and the stage calculation module,
the design method comprises the following steps:
(1) the data input module inputs the score to be dividedFraction t of fraction A to be separated1、A2、…、AtCoefficient of separation between components to be separated
Figure FDA0003330892150000012
The requirements for impurities and calculation accuracy in the final product are met;
(2) the flow calculation module constructs a full separation flow chart according to the components to be separated and the number of the components, which are input by the data input module, and calculates the minimum extraction amount, the minimum washing amount, the total material flow of outlets at two ends and the component flow of each component in the full separation flow chart from top to bottom level by level, and the input and output material total flow and the component flow of each component in the input and output material total flow of a connection level after the outlets of adjacent separation units at the same level are linked;
(3) calculating the number of extraction stages and the number of washing stages required by each separation unit by the number-of-stages calculation module;
(4) the result output module outputs a full separation flow chart with flow data and stage data and a percentage content change chart of components contained in each stage material in two phases according to the calculation results of the flow calculation module and the stage calculation module;
(5) according to the lowest separation level, namely the calculation result of the separation level containing 2 components in the used feed liquid, the minimum extraction amount and the minimum washing amount of the multi-component linkage extraction separation process are determined in a gathering way,
wherein:
in the step (2),
for the type I separation unit, when the used feed liquid is an aqueous phase, the calculation formulas of the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets at two ends and the flow of each component in the total flow are respectively as follows:
Figure FDA0003330892150000021
Figure FDA0003330892150000022
Figure FDA0003330892150000023
Figure FDA0003330892150000024
wherein i is more than or equal to 1 and less than or equal to t, and:
Sminminimum extract;
Wminis the minimum wash load;
Figure FDA0003330892150000029
is A1And AtThe separation factor between the two components;
Figure FDA00033308921500000210
is AiAnd AtThe separation factor between the two components;
Figure FDA0003330892150000025
is AiThe flow rate of the components in the aqueous phase feed liquid is
Figure FDA0003330892150000026
Figure FDA0003330892150000027
And
Figure FDA0003330892150000028
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure FDA0003330892150000031
and
Figure FDA0003330892150000032
the total flow of all components in the water phase flowing out of the 1 st level and the total flow of all components in the organic phase flowing out of the n + m level are respectively obtained before linkage connection;
for the type I separation unit, when the used feed liquid is an organic phase, the calculation formulas of the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets at two ends and the flow of each component in the total flow are respectively as follows:
Figure FDA0003330892150000033
Figure FDA0003330892150000034
Figure FDA0003330892150000035
Figure FDA0003330892150000036
wherein:
Sminminimum extract;
Wminis the minimum wash load;
Figure FDA0003330892150000037
is A1And AtThe separation factor between the two components;
Figure FDA0003330892150000038
is A1And AiThe separation factor between the two components;
Figure FDA0003330892150000039
is AiFlow rate of the components in the organic phase feed liquid, and
Figure FDA00033308921500000310
Figure FDA00033308921500000311
and
Figure FDA00033308921500000312
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure FDA00033308921500000313
and
Figure FDA00033308921500000314
the total flow of all components in the water phase flowing out of the 1 st level and the total flow of all components in the organic phase flowing out of the n + m level are respectively obtained before linkage connection;
for the type I separation unit, when the used feed liquid is two feed liquids of a water phase and an organic phase, the calculation formulas of the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets at two ends and the flow of each component in the total flow are respectively as follows:
Figure FDA0003330892150000041
Figure FDA0003330892150000042
Figure FDA0003330892150000043
Figure FDA0003330892150000044
wherein:
Sminminimum extract;
Wminis the minimum wash load;
Figure FDA0003330892150000045
is A1And AtThe separation factor between the two components;
Figure FDA0003330892150000046
is A1And AiThe separation factor between the two components;
Figure FDA0003330892150000047
is AiAnd AtThe separation factor between the two components;
Figure FDA0003330892150000048
is AiThe flow rate of the components in the aqueous phase feed liquid;
Figure FDA0003330892150000049
is AiThe flow rate of the components in the organic phase feed liquid;
Figure FDA00033308921500000410
and
Figure FDA00033308921500000411
respectively before linkage connection AiThe flow rate of the aqueous phase of which the components flow out of the 1 st stage and the flow rate of the organic phase of which the components flow out of the n + m th stage;
Figure FDA00033308921500000412
and
Figure FDA00033308921500000413
the total flow of all components in the water phase flowing out of the 1 st level and the total flow of all components in the organic phase flowing out of the n + m level are respectively obtained before linkage connection;
for the II-type separation unit, the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets at two ends and the flow calculation formulas of all the components are respectively as follows:
Figure FDA00033308921500000414
Figure FDA0003330892150000051
Figure FDA0003330892150000052
Figure FDA0003330892150000053
wherein p is not less than i not more than q and:
Sminminimum extract;
Wminis the minimum wash load;
Apand AqAre respectively a separation unit materialThe components with the minimum number and the maximum number in the liquid;
Figure FDA0003330892150000054
is ApAnd AqThe separation factor between the two components;
Figure FDA0003330892150000055
is ApAnd AiThe separation factor between the two components;
Figure FDA0003330892150000056
is AiAnd AqThe separation factor between the two components;
Figure FDA0003330892150000057
is AiThe flow rate of the components in the aqueous phase feed liquid;
Figure FDA0003330892150000058
and
Figure FDA0003330892150000059
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure FDA00033308921500000510
and
Figure FDA00033308921500000511
the total flow of all components in the water phase flowing out of the 1 st level and the total flow of all components in the organic phase flowing out of the n + m level are respectively obtained before linkage connection;
Figure FDA00033308921500000512
a in the organic phase of a separation unit for providing feed liquid from a feed stage to a high stageiThe split flow of the components;
ysumthe sum of the flow rates of all components in the organic phase of the separation unit, which provides the feed liquid for extraction from the feed stage to the upper stage, and having:
ysum＝(Smin)H (27)
wherein (S)min)HTo provide the minimum extraction capacity required for the high level separation unit of the feed solution,
for the III-type separation unit, the minimum extraction amount, the minimum washing amount, the total flow of materials at two ends and the flow of each component in the total flow are respectively calculated by the following formulas:
Figure FDA0003330892150000061
Figure FDA0003330892150000062
Figure FDA0003330892150000063
Figure FDA0003330892150000064
wherein p is not less than i not more than q and:
Sminminimum extract;
Wminis the minimum wash load;
Apand AqRespectively the components with the minimum number and the maximum number in the feed liquid of the separation unit;
Figure FDA0003330892150000065
is ApAnd AqThe separation factor between the two components;
Figure FDA0003330892150000066
is ApAnd AiThe separation factor between the two components;
Figure FDA0003330892150000067
is AiAnd AqThe separation factor between the two components;
Figure FDA0003330892150000068
is AiThe flow rate of the components in the organic phase feed liquid;
Figure FDA0003330892150000069
and
Figure FDA00033308921500000610
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure FDA00033308921500000611
and
Figure FDA00033308921500000612
the total flow of all components in the water phase flowing out of the 1 st level and the total flow of all components in the organic phase flowing out of the n + m level are respectively obtained before linkage connection;
Figure FDA00033308921500000613
providing A in the aqueous phase flow of the feed liquid separation unit for extraction from the feed stage to the high-stageiThe split flow of the components;
xsumproviding the sum of the flow rates of all components in the aqueous phase stream of the feed liquid separation unit for extraction from the feed stage to the upper stage, and having:
xsum＝(Wmin)H (34)
wherein (W)min)HTo provide the minimum amount of washing required by the high level separation unit of the feed solution.
2. The method of claim 1, wherein in step (1), the separation coefficient between the components to be separated
Figure FDA0003330892150000071
For any two components AiAnd Aj，1≤i<j is less than or equal to t, and separation coefficient between
Figure FDA0003330892150000072
Calculated from the following formula:
Figure FDA0003330892150000073
wherein i is more than or equal to 1 and j is less than or equal to t.
3. The design method according to claim 1, wherein in step (2), for two adjacent separation units located at the same level, the organic phase outlet of the previous separation unit L is connected with the aqueous phase outlet of the next separation unit R, the separation unit L provides the extraction organic phase for the separation unit R, meanwhile, the separation unit R provides the washing liquid for the separation unit L, the input and output material total flow and each component flow therein of the subsequent connection stage are connected, and the total material flow and each component flow therein of the subsequent connection stage are connected and output to the next separation level are calculated as follows:
1) first, compare
Figure FDA0003330892150000074
And (S)min)R、
Figure FDA0003330892150000075
And (W)min)LA size of between, wherein
Figure FDA0003330892150000076
And (W)min)LRespectively representing the total flow of the components of the organic phase outlet and the minimum washing quantity required before the linkage of the separation unit L,
Figure FDA0003330892150000077
and (S)min)RRespectively representing the total flow of all components of the water phase outlet and the required minimum extraction amount before the linkage of the separation unit R;
2) the comparison results show the following three cases:
Figure FDA0003330892150000078
Figure FDA0003330892150000081
Figure FDA0003330892150000082
3) in the first case, when both (35) and (36) are simultaneously established, the organic phase outlet flow (y) of the separation unit L is linked and connectedsum,n+m)LCalculated as follows:
Figure FDA0003330892150000083
linked connected aqueous phase outlet flow (x) of the rear separation unit Rsum,1)RCalculated as follows:
Figure FDA0003330892150000084
in this case, after linkage connection, if the net output organic phase contains only 1 component, that is, is taken out as a product, and if the net output organic phase contains more than 1 component, the next-stage phase-connected type IV separation unit is provided as a feed liquid, and the total flow rate f of the feed liquidoCalculated as follows:
Figure FDA0003330892150000085
wherein the split flow of each component
Figure FDA0003330892150000086
Calculated as follows:
Figure FDA0003330892150000087
wherein,
Figure FDA0003330892150000088
the split flow of each component in the organic phase outlet before the linkage of the separation unit L,
Figure FDA0003330892150000089
the component flow of each component in the water phase outlet before the linkage of the separation unit R;
4) in the second case, when both (37) and (38) are simultaneously established, the outlet flow (y) of the organic phase of the separation unit L is linked and connectedsum,n+m)LCalculated as follows:
Figure FDA00033308921500000810
separating sheet after linkage connectionWater phase outlet flow (x) of element Rsum,1)RCalculated as follows:
Figure FDA00033308921500000811
after linkage connection, if the net produced water phase only contains 1 component, namely the water phase is taken out as a product, and if the net produced water phase contains more than 1 component, the next level connected IV type separation unit is provided as a feed liquid, and the total flow rate f of the feed liquidaCalculated as follows:
Figure FDA0003330892150000091
wherein the split flow of each component
Figure FDA0003330892150000092
Calculated as follows:
Figure FDA0003330892150000093
wherein,
Figure FDA0003330892150000094
the split flow of each component in the organic phase outlet before the linkage of the separation unit L,
Figure FDA0003330892150000095
the component flow of each component in the water phase outlet before the linkage of the separation unit R;
5) the third situation is that when the two types (39) and (40) are simultaneously established, the organic phase outlet flow (y) of the separation unit L is linked and connectedsum,n+m)LCalculated as follows:
Figure FDA0003330892150000096
linked connected aqueous phase outlet flow (x) of the rear separation unit Rsum,1)RCalculated as follows:
Figure FDA0003330892150000097
after linkage connection, if the net produced water phase and organic phase only contain 1 component, namely the net produced water phase and organic phase are taken out as products, if the net produced components contain more than 1 component, the water phase and organic phase feed liquid is simultaneously provided for the IV type separation unit connected with the next layer, and the total flow f of the water phase and the organic phase feed liquid is respectivelyaAnd foThe calculation is carried out according to the following two formulas:
Figure FDA0003330892150000098
Figure FDA0003330892150000099
wherein the flow rates of the components in the aqueous phase and organic phase feed liquid are divided
Figure FDA00033308921500000910
And
Figure FDA00033308921500000911
the calculation is carried out according to the following two formulas:
Figure FDA00033308921500000912
Figure FDA00033308921500000913
wherein,
Figure FDA0003330892150000101
the split flow of each component in the organic phase outlet before the linkage of the separation unit L,
Figure FDA0003330892150000102
is the split flow of each component in the water phase outlet before the linkage of the separation unit R.
4. The design method according to claim 1, wherein, in the step (2),
for the IV separation unit, the used feed liquid is from the material which is net output after the outlets of two adjacent separation units in the previous separation level claim 3 are linked, and the calculation method of the minimum extraction amount, the minimum washing amount, the total flow of the materials at the outlets at two ends and the flow of each component in the material is as follows:
1) when the feed liquid provided by the previous separation level is a water phase, calculating according to the formulas (21) to (27) by adopting a water phase feeding level linkage mode;
2) when the feed liquid provided by the previous separation level is an organic phase, calculating according to the formulas (28) to (34) by adopting an organic phase feeding level linkage mode;
3) when the feed liquid provided by the previous separation level is two feed liquids of a water phase and an organic phase, calculating according to the following formula;
Figure FDA0003330892150000103
Figure FDA0003330892150000104
Figure FDA0003330892150000105
Figure FDA0003330892150000106
wherein p is not less than i not more than q and:
Sminminimum extract;
Wminis the minimum wash load;
Apand AqRespectively the components with the minimum number and the maximum number in the feed liquid of the separation unit;
Figure FDA0003330892150000111
is ApAnd AqThe separation factor between the two components;
Figure FDA0003330892150000112
is ApAnd AiThe separation factor between the two components;
Figure FDA0003330892150000113
is AiAnd AqThe separation factor between the two components;
Figure FDA0003330892150000114
is AiThe flow rate of the components in the aqueous phase feed liquid;
Figure FDA0003330892150000115
is AiThe flow rate of the components in the organic phase feed liquid;
Figure FDA0003330892150000116
and
Figure FDA0003330892150000117
respectively before linkage connection AiThe flow rate of the aqueous phase from which the components flow out of the 1 st stage and the flow rate of the organic phase from which the components flow out of the n + m th stage;
Figure FDA0003330892150000118
and
Figure FDA0003330892150000119
the total flow of all components flowing out of the water phase of the 1 st stage and the total flow of all components flowing out of the organic phase of the n + m th stage before linkage connection are respectively.
5. The design method according to claim 3, wherein in the step (2), when the total flow of the input and output materials and the flow of each component in the input and output materials of the connection stage after the outlets of two adjacent separation units in the same stage are linked, the number of the components in the feed liquid of the stage is 2, that is, the separation stage is located at the lowest separation stage, and the two formulas (35) and (36) are simultaneously satisfied, a blank washing liquid needs to be supplemented to the separation unit L, and the flow of the supplemented blank washing liquid is calculated according to the following formula:
Figure FDA00033308921500001110
wherein,
(Wadd)La newly added flow of blank wash liquid for the separation unit L;
(Wmin)Lrepresents the minimum amount of washing required for the separation unit L;
Figure FDA00033308921500001111
and (S)min)RRespectively representing the total flow of each component of the water phase outlet and the required minimum extraction amount before the linkage of the separation unit R.
6. The design method according to claim 3, wherein in the step (2), when the total flow of the input and output materials and the flow of each component in the input and output materials of the connection stage after the mutual outlet linkage between two adjacent separation units in the same level is calculated, the component number in the material liquid of the level is 2, namely the separation stage is located at the lowest separation level, and the two formulas (37) and (38) are simultaneously satisfied, then the separation unit R is supplemented with the blank extraction organic phase, and the flow of the supplemented blank extraction organic phase is calculated according to the following formula:
Figure FDA0003330892150000122
wherein,
(Sadd)Rextracting the organic phase flow for the newly added blank of the separation unit R;
(Smin)Rrepresents the minimum extraction required for the separation unit R;
Figure FDA0003330892150000121
and (W)min)LRespectively representing the total flow of the components of the organic phase outlet and the minimum washing quantity required before the separation unit L is coupled.
7. The design method according to claim 1, wherein in the step (5), the total minimum extraction amount and the total minimum washing amount required by the whole separation process are determined in a summary manner according to the calculation results of the separation levels of 2 components in the feed liquid, and the method comprises the following steps:
the total minimum extraction amount is equal to the sum of the minimum extraction amount of the type II separation unit at the lowest level and the flow of the blank extraction organic phase which needs to be supplemented after the outlets of all adjacent separation units at the lowest level are linked;
the total minimum washing amount is equal to the sum of the minimum washing amount of the type III separation unit at the lowest level and the flow of the blank washing liquid needing to be supplemented after the outlets of all the adjacent separation units at the lowest level are linked and connected.
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