Method and instrument for material desorption

FIELD: chemistry.

SUBSTANCE: in invention claimed are devices and methods for continuous anti-current desorption of target materials. Device for substance desorption from ion-exchange resin which has sorbated on it admixtures and target materials, includes first and second chamber. Resin is supplied into first chamber, and is transported from first chamber to second chamber, and desorbing solution is supplied into second chamber, and is transported from second chamber into first chamber. Admixtures, which have less affinity with resin, than target material, can be desorbed from resin, and target material can be sorbed on resin from desorbing solution in first chamber. Flow of admixtures, which has high admixture concentration and relatively low concentration of target material, is released from first chamber through first outlet. Target material is desorbed from resin in second chamber, and enriched flow, which has low admixture concentration and relatively high concentration of target material, is released from low parts of first and/or second chamber through second outlet.

EFFECT: extension of arsenal of means for substance desorption from ion-exchanging resin.

41 cl, 6 dwg, 1 tbl, 5 ex

 

The technical FIELD TO WHICH the INVENTION RELATES.

The present invention relates to a method and apparatus for desorption of material from a saturated ion-exchange resin.

The ion-exchange resin may be any suitable resin, which may be saturated target materials, which include non-ferrous metals, such as copper, Nickel and cobalt; noble metals such as gold and silver; and refractory metals such as molybdenum and tungsten. The ion-exchange resin may also be suitable for any other metal, non-metal, organic compounds, inorganic compounds, and mixtures thereof.

The prior art INVENTIONS

Currently there is a wide variety of technologies that can be used for desorption of materials from resins. Some technologies are more suitable than others for specific applications, and therefore the selection of the most appropriate technology is an important factor in achieving high speed desorption and cost-effectiveness.

Generally speaking, the processes of desorption for deformirovaniya material from the resin can be conducted as a batch or continuous operations, which typically correspond to apparatus for carrying out processes with so-called fixed layers or moving layers.

Devices with a fixed layers currently the most is its widely used in the industry. For example, the publication Abrams I.M., entitled "Type of ion-exchange system" (Ion Exchange for Pollution Control, eds. C.Calmon and H.Gold, CRC Press, Boca Raton, vol.1, pp.71-850, 1979), describes that the processing unit with a fixed layer worked for more than 25 years and is currently still used for softening 1500 megalitres per day of water in the Metropolitan Water District of southern California.

Publication Salem E., entitled "Equipment operation and design" (Ion Exchange for Pollution Control, eds. C.Calmon and H.Gold, CRC Press, Boca Raton, vol.1, pp.87-100, 1979), describes that the desorption cycle of the majority of vehicles with a fixed layer includes: initial backwash layer is fully saturated, or saturated resin, defending layer; passing the Stripping solution through the layer; removing the Stripping solution (or slow rinse), and finally rinse the resin before applying the rich solution on the layer.

Stage backwashing removes suspended solids that have accumulated in the resin layer, and eliminates the channels could be formed during the stage of sorption. Backwashing also helps to break up the agglomerates formed by suspended particles and ion exchange resins.

Stage sedimentation is followed by stage backwashing and important in order to avoid channeling of the flow through the layer.

Desorption is carried out by passing the desorption solution cher the C layer, converting the resin into a desired shape. Once the appropriate volume of desorption solution provisionally resin is removed desorption solution of the layer.

Rinse the resin demineralized water is usually used to remove the last remnants of desorption solution of the layer.

Upon completion stage of leaching liquid phase containing the target material, subject to sorption on the resin during the stage of sorption, enters the upper part of the column, when the column operates in continuous mode, or on the bottom of the column when the column operates in counterflow mode.

U.S. patent No. 4412866 describes the modification of a periodic fashion with a fixed layer, in particular, relates to a simulated active layer, in which the separate zones, each of which includes one or more separate containers. The zones correspond to the functions of the method; usually sorption, removal, desorption and leaching. Auxiliary pumps are connected in series with the containers that support the desired value of the pressure in each zone. The functions of each of the zones alternate in sequence, and the sequence schedule relative to the moving front between adjacent phases in the loop flow circulating through the area.

Another type of adsorption/desorption of ways you submitted the continuous method. Generally speaking, the adsorption/desorption method can be classified as continuous way, when sorption, leaching and desorption are carried out simultaneously, and product flow is continuous. The use of the rolling layer of resin makes it possible to achieve continuous operation, and the main advantage is the high efficiency of the process.

As periodic methods, continuous methods can work in a co-current or counter-current.

Not all methods are described as continuous, are indeed continuous ways. Really continuous methods work without interrupting the flow of the resin or liquid. Semi-continuous methods often have a short constant period in which the absorption (i.e. the mode), followed by a period when the resin is moving (motion). However, as the periods for both modes is very short, the method actually works as continuous. We know more than hundreds of semi-continuous methods, but only about six have some real commercial significance.

In our opinion the most widely known method of this type is the so-called loop Higgins (described in the publication Higgins, I.R. and Roberts, I.t. "A countercurrent solid-liquid contactor for continuous ion-exchange. Eng Pog. Symp. Ser., 50, 87-94, 1950). Loop Higgins is a continuous iwny countercurrent ion-exchange method for separating the liquid phase from the ionic components using solid ion-exchange resin.

Loop Higgins includes a vertical cylindrical vessel containing a Packed layer of ion exchange resin, which is divided into four work areas swivel or hinge flaps. These work areas - adsorption, desorption, backwashing and ripple - operate as four separate container.

Loop Higgins handles liquid resin in the area of sorption, ions while simultaneously removed from the saturated resin in the desorption zone. Periodically a small portion of the resin is removed from the corresponding zone and replaced desorbed or saturated with resin on the opposite end of this area. This is achieved hydraulically ripple resin through the loop. The result is a continuous method in which the liquid and the resin are in contact in counter-current mode.

The aim of the present invention is the provision of an alternative method and apparatus for desorption of materials adsorbed on the resin capable of giving a stream of concentrated eluate.

The INVENTION

According to the present invention features apparatus for desorption of the compounds from the ion-exchange resin having adsorbed impurities and target material, and the apparatus includes:

the first and second chambers, which are made so that when the resin is supplied into the first chamber and is moved from the first is the first camera to the second camera, and deformirujuschij solution is fed into the second chamber and is moved from the second chamber into the first chamber so that

i) impurities having a lower affinity for the resin than the target material, can decorrelates from the resin, and the target material may absorb the resin from the Stripping solution, and thus to create conditions where the flow of impurities with a high concentration of impurities and a relatively low concentration of the target material can be discharged from the first chamber, and

ii) the target material can decorrelates from the resin in the second chamber, and to create conditions where enriched stream with a low impurity concentration and a relatively high concentration of the target material can be produced from the lower parts of the first and/or second chambers.

In addition, when the apparatus is in operation, preferably, when the resin flows down in the first chamber and up the second camera, and when deformirujuschij solution flows in countercurrent to the direction of flow of the resin in the above-mentioned cameras.

Even more preferably, when the flow of impurities released from the upper part of the first chamber.

Preferably, when the first and second flow chambers are connected by the connection so that deformirujuschij solution may flow from the first chamber into the second chamber.

According to the present invention it is also proposed devices is for desorption of material from a saturated ion exchange resin, moreover, the apparatus includes:

the first and the second camera, which is arranged so that when the resin may move down in the first chamber and up the second camera, and deformirujuschij solution can flow in countercurrent to the resin;

the first and second inputs for supplying saturated resin into the first chamber and the Stripping solution into the second chamber, respectively, and first and second outputs for draining liquid from the apparatus and desorbed resin from the second chamber, respectively;

the means of ensuring the transfer of resin from the first chamber into the second chamber and moving the resin up in the second chamber; and

when the first thread Stripping solution containing a relatively high impurity concentration and a low concentration of the target material, can be produced from the first output, the second thread Stripping solution containing a relatively high concentration of the target material and a low concentration of impurities can be discharged through the first outlet from the lower parts of the first and/or second chambers and/or be selected from the Stripping solution passing from the second chamber into the first chamber, and desorbed resin can be produced from the second output of the second camera.

The advantages provided by the present invention include:

ii) impurities having a lower affinity for the resin than C is left material, desorbers from the resin before the target material, and therefore the first thread Stripping solution has a higher concentration of impurities and can be produced from the first chamber, where deformirujuschij the first solution comes in contact with the resin;

iii) after desorption of impurities from the resin tank resin by the absorption of the target material increases, which allows the first camera to have an area for readable target material on the resin; and

iv) target materials desorbed from the resin, fall in deformirujuschij solution, and, thus, increases the density of the solution so that it has a tendency to settle under gravity in the cells and, thus, helps the second thread Stripping solution containing a relatively high concentration of the target substance and a low concentration of impurities, leaving the lower part of the device.

Preferably, when the desorption of impurities from the resin occurs in the upper zone of the first chamber and, thus, allows for the sorption of target material on the resin in the upper zone. In other words, the upper zone creates a zone of readable.

Preferably, when the first and second chambers are connected flow-through connection so that the pressure fluid in the second chamber causes deformirujuschij solution to flow upwards in the first chamber.

You should take into attention to detail is e, as a result of the filing of the Stripping solution in the second chamber predominant direction of flow Stripping solution is directed from the second chamber into the first chamber. You must also take into account that the total upward flow of Stripping solution in the first chamber will be essentially equal to the flow rate with which the first thread Stripping solution is discharged from the first chamber.

Preferably, when the first outlet for the first flow of the Stripping solution is in the upper part of the first chamber. The advantage of this preferred characteristic is that deformirujuschij the first solution comes in contact with the resin in the upper part of the first chamber, and an impurity having a lower affinity for the resin than the target material can be discharged from the upper end of the first chamber.

Preferably, when the second output for the release of desorbed resin is located in the upper part of the second camera. The advantage of this preferred object, is that the resin gradually interacts with desorbers solution having a low concentration of the target material as the resin moves up in the second chamber and, thus, creates a greater potential for desorption of the target materials from the resin in the second chamber before the resin is going to be released from the device.

Preferably, when the flow is directed downwards from the second output to move desorbed resin in the intermediate chamber before release of the device.

Preferably, when the first and second inputs for desorbed resin and Stripping solution into first and second chambers respectively located in the upper parts of the chambers.

Preferably, when the apparatus has means of control for controlling the speed of removal of the resin from the second chamber. When the work tool control and measure the level of liquid Stripping solution in the first chamber to regulate the flow rate with which the resin is removed from the second chamber.

Preferably, when the second camera has another input for supplying a concentrated solution of the target material into the second chamber. The authors found that the addition of concentrated solution into the second chamber increases the concentration of the target material in the second stream Stripping solution (i.e. the flow of the eluate) and reduces the concentration of impurities in the second stream.

Now will be described the preferred characteristics of the two embodiments of the present invention.

Preferably, when the first and second chambers connected by the flow, which extends from the first chamber to the second chamber, and Pareto is designed to transfer the resin and Stripping solution between cameras.

According to one variant of implementation of the present invention preferably also, when the first and second chambers are connected in a U-shape having a base and two shoulder where the first and second chambers form the shoulders of the U-shaped base provides the flow.

Preferably, when the second thread Stripping solution containing a high concentration of desorbed material discharged from the overflow, which is located between the first and second chambers. When the first and the second chamber is connected in a U-shape, the second thread Stripping solution having a high concentration of the target material, produced from the base of the U-shaped form.

According to another variant of the invention, preferably, when the first and second chambers are arranged so that one camera is inside another camera.

Even more preferably, when the second camera is located concentrically in the first chamber.

When the second camera is located inside the first chamber, it is preferable that the second chamber had a hole open down to deformirujuschij solution from the first chamber can flow into the second chamber, and that the resin from the second chamber was entered into the first chamber through the hole and was forced to move up in it.

Preferably, when the second is OK Stripping solution discharged from the first chamber in place, located below the openings of the second camera.

Preferably, when the bottom wall of the first chamber is inclined in the direction of output to produce a second stream Stripping solution having a high concentration of target compounds.

According to the present invention offers a method for desorption of the compounds from the ion-exchange resin having adsorbed therein impurities and target material, and the method includes processing the ion exchange resin in the apparatus having first and second chambers, where the method includes the following stages:

a) desorption of impurities from the resin in the first chamber with the use of Stripping solution so that the target material has a greater affinity for the resin than the impurities, can absorb on the resin from the Stripping solution, and, thus, conditions are created when a thread having a high impurity concentration and a low concentration of the target material, can be produced from the first chamber; and

b) desorption of the target materials from the resin treated according to stage a), the second camera with the use of Stripping solution and, thus, the creation of conditions when the stream having a high concentration of the target material and a low concentration of impurities, can be produced from the device.

According to the present invention also proposes a method for desorb the AI substances from the resin in the apparatus, with the first and second camera associated with running connection, and the method includes the steps:

a) feeding a saturated resin having adsorbed therein a target material and impurities into the first chamber and the movement of the resin down at her.

b) the movement of resin from the first chamber into the second chamber and the movement of the resin up to her.

(C) filing Stripping solution into the second chamber so that the solution flows down the second chamber and up into the first chamber in countercurrent to the resin;

d) release of desorbed resin from the second camera;

e) release the first thread Stripping solution containing a high impurity concentration and a low concentration of the target substance from the first chamber; and

f) release the second thread Stripping solution containing a relatively high concentration of the target material and the relatively low concentration of impurities from the bottom of the first and/or second chambers and/or from a solution, moving between cameras.

Preferably, when any two or more of the steps from a) to f) are performed simultaneously.

Preferably, when the impurities in the resin have a lower affinity for the resin than the target material, so that when the resin is in contact with desorbers solution in the first chamber, impurities tend to decorrelates from the resin before desorption of the target materials.

Site is preferably, when the desorption of impurities from the resin occurs in the upper zone of the first chamber and, thus, allows an additional target material absorb on the resin in the upper zone.

Preferably therefore, when the first stream is produced at stage (e)is produced in the upper part of the first chamber.

Preferably, when the target material desorbed from the resin and dissolved in the solution, increase the density of the solution, thus, causing the fraction of a solution having a high concentration of target compounds, to settle under gravity in the bottom of the first and second chambers.

Therefore, preferably, when the second stream is produced at stage f), released from the solution, moving between cameras, or from the lower parts of the first and/or second chambers.

Preferably, when the flow rate with which the resin produced in stage (d), adjusting the level of fluid in the first chamber.

Preferably, when the resin, produced by stage (d), released from the upper parts of the second chamber.

Preferably, when the method also includes the supply of a concentrated solution of the target substance in the second chamber. The authors found that the addition of a solution of concentrated substances into the second chamber increases the concentration of the target substance in the second thread Stripping solution is (i.e. the flow of the eluate) and reduces the concentration of impurities in the second stream.

Preferably, when the temperature of the concentrated solution is in the range of approximately 60 to 100°C.

Preferably, when the additional solution serves the second chamber in the space between the upper and lower parts of the second chamber.

The method of the present invention may also include any of the features of the apparatus described above.

BRIEF DESCRIPTION of DRAWINGS

Two preferred alternative implementation of the present invention will now be described with reference to the accompanying drawings, of which:

figure 1 depicts apparatus for desorption of material from the resin according to one variant embodiment of the invention in which the apparatus includes two cameras, with one camera is inside the other;

2 and 3 depict an implementation option, shown in figure 1, with additional signs;

figure 4 depicts apparatus for desorption of material from the resin according to the alternative implementation in which the device includes two cameras that are connected in a U-shape; and

5 and 6 depict an implementation option, shown in figure 4, with additional signs.

A DETAILED DESCRIPTION of the PREFERRED embodiments

Two preferred option implemented is I have a number of common characteristics, and the same item numbers are used to designate the same or similar characteristics in both cases, the implementation, where possible.

The preferred implementation shown in figure 1, contains a device having two cameras, of which the inner chamber 1 is located concentrically in the outer chamber 2.

Inner chamber 1 has an inlet valve 14 to supply Stripping solution into the internal chamber and an outlet for desorbed resin. From the outlet is directed pipe that directs desorbed resin in the intermediate tank 7. The lower end of the inner chamber 1 has an opening opened downward so that deformirujuschij solution flows downward in the inner chamber 1 and upwards in the outer chamber 2 in the direction of the dotted arrows.

The pressure of the liquid Stripping solution in the inner chamber 1 causes deformirujuschij solution to flow upwards in the outer chamber 2.

External camera 2 has a resin or pipe 5 for supplying saturated resin in the outer chamber 2. The resin in the outer chamber 2 moves downward in the direction of the arrows, shown with continuous lines, in countercurrent to desorbers solution. The resin also perelavlivaet through the opening into the internal chamber 1 and moves up in the inner chamber 1 in the direction of the arrows, shown with continuous lines, in countercurrent to desorber usamu solution.

When working the saturated resin enters through the tube 5 and is connected with a saturated resin in the upper part of the outer chamber 2. First impurities having a lower affinity for the resin than the target material, desorbers from the resin. As a result, the flow of the Stripping solution having a high concentration of impurities, is produced through the outlet pipe 3.

After desorption of the impurities remains resin, and the capacity of this resin in the ratio of sorption of the target material can be increased so that the top of the outer chamber 1, in which deformirovanii impurities, may also form a zone of readable target material on the resin. Usually the area of readable formed in the upper part of the first chamber 1, supports the concentration of the target material low in thread Stripping solution is released through the outlet pipe 3.

The saturated resin moves down after readable and into the internal chamber 1, where the target material is desorbed in the desorption zone of the device.

Resin moves along the inner and outer chambers 1 and 2, using any suitable means, such as ripple resin. In the case of the variant implementation, shown in figure 1-3, the pulsation of the resin is carried out, opening the valve 13 for releasing the resin from the apparatus by closing the valve 14 with the interruption Stripping solution and pumping air into the colon is through the tube 6, located in the upper part of the zone of readable.

The electrodes 9 and 10, which measure the level of the Stripping solution in the outer chamber 2, perform hardware control the speed at which the resin is removed from the apparatus. The movement of the resin in the chambers 1 and 2 can occur periodically, once every 0.5-3.0 hours and continue for 0.5-2.0 minutes, depending on the properties of the resin, the target material and method of desorption.

Deformirujuschij solution is pumped into the internal chamber 1 through the pipe 4 and the valve 14. Deformirujuschij the solution retrieves the target material from the saturated resin during its movement after the desorption zone 1 down to the bottom of the device. Thread Stripping solution containing a high concentration of the target material and a low concentration of impurities released from the bottom of the apparatus through the pipe 8. The flow of solution from the bottom of the Cabinet regulate by means of a valve 15.

The strainer 11 at the bottom of the device holds the resin in the outer chamber 2, while the solution release.

2 and 3 depict the apparatus shown in figure 1, having an inlet 12 for supplying a concentrated solution of the target material in the middle of the inner chamber 1. The authors found that the addition of concentrated solution in the inner chamber 1 reduces the concentration of impurities and increases the concentration of the target material produced by the th of the apparatus through the valve 15.

Figure 3 depicts the device equipped with heat exchange means for preheating Stripping solution supplied into the internal chamber 1 through the inlet 12 and the valve 14 to facilitate desorption of material from the resin in deformirujuschij solution. Deformirujuschij the solution is preferably heated to a temperature in the range from 60 to 100°C.

The apparatus also includes an external insulation to maintain the temperature of the Stripping solution in the chambers 1 and 2.

Figure 4 depicts an alternative implementation, in which the camera 1 and 2 are connected in a U-shape. More specifically, the camera pulled upward from opposite ends of the horizontal flow that connects the camera. The diameter of the flow is essentially the same as the diameter of the chambers 1 and 2, so that the resin can be moved from chamber 2 into chamber 1 with the use of technology pulsations described above.

Flow also provides a flow connection between the chambers 1 and 2 so that the pressure of the liquid Stripping solution in the chamber 1 causes deformirujuschij solution to flow upwards in the chamber 2.

Moreover, an implementation option, shown in figure 4-6 includes the same characteristics as an implementation option, shown in figure 1-3, and can work the same way. The same item numbers are used in both versions of the implementation in order to show the same signs.

Provided that embodiments of the present invention can function in such a way that the resin and deformirujuschij solution flow continuously in countercurrent. However, specialists in the art should take into account that during the Stripping solution and the movement of the resin can be pulsating, and, generally speaking, continuous desorption is a method in which the resin moves pulsations through desorption apparatus. In particular, the movement of the resin in desorbers the apparatus generally includes a resin layer moving along uneven steps, whereby the resin tube emerges from the end of the layer and the remainder of the resin moves in the direction along the layer.

The present invention will now be described with reference to the following non-limiting examples.

EXAMPLE 1

This example illustrates the desorption of copper from the resin, which was filled during processing wastewater flows galvanizing plant copper coating. The example is implemented using the apparatus, the construction of which is shown in figure 4.

Copper concentration in the wash water was approximately 50-80 hours/million, and the capacity of saturation of the resin reached 28-32 g/l

Desorption the experiment was carried out in 150 l plastic U-shaped column according to a variant implementation, shown in figure 4. The saturated resin come in the and in the column through the tube 5, located on the lid of the column. After desorption fully purified resin was removed hourly from the column through the outlet pipe and the intermediate tank 7. The resin passed through the column with a flow rate of 20 l/h

7% solution of sulfuric acid was used as Stripping solution. Deformirujuschij stream was pumped with a flow rate of about 22 l/h in the upper part of the desorption zone of the column through a tube 4 with the valve 14 in the open state.

The waste stream is removed through a drain 3 with a flow rate of 11.5 to 12.5 l/h copper Concentration in the exhaust stream was less than 200 hours/million and returned with flushing water through sorption.

The flow of the eluate were collected from the bottom of the column through the lattice filter 11 and the pipe 8. The solution of the eluate were collected with a flow rate of 9.5-10.5 l/h through the valve 15. Copper concentration in the flow of the eluate reached 60 g/l, very close to the maximum solubility of copper sulfate (CuSO4·5H2O) (copper sulphate). This flow of the eluate analytically and economically suitable for direct extraction of copper using well known methods, such as electrochemical recovery of copper or deposition of copper sulphate.

It is assumed that the flow of the eluate obtained in the above example, can be used directly in the copper electrolytic bath, and waste wash water containing copper, may be returned to manufacturers who only cycle galvanizing plant copper coating. It is also assumed that the treated water can be returned to the water system galvanizing plant copper coating.

EXAMPLE 2

This example illustrates the desorption of Nickel from the resin, which was filled during the sorption of Nickel of autoclaved sludge leaching of laterite. The example is implemented using the apparatus shown in figure 4.

Elemental analysis of the saturated resin shown in the table.

Desorption equipment consisted of a U-shaped plastic laboratory columns with a volume of 750 ml Resin flowed through the column with a flow rate of 100 ml/h

10% solution of hydrochloric acid was used as desorbers liquid. The solution was pumped into the column through the pipe 4 and the valve 14 and flowed through a desorption zone and readable with a flow rate of 160 ml/h Flow Stripping solution was divided into two unequal parts:

i) the waste Stream solution, which was collected after desorption from the effluent 3 with a volume flow of about 100 ml/h and was sent to the stage sorption together with rich sludge leaching.

ii) flow of the eluate, which was collected from the bottom of the column through a pipe 15 and a partially open valve 8 with a volume flow rate of 60 ml/h Elemental analysis for flow of the eluate and sinks below the table.

Table

Financial p the tats elemental analysis of initial and final products
The saturated resin, g/lThe flow of the eluate, h/millionThe flow of impurities, am/million
Ni36,8159510382
Co1,651460493
Mn2,167012750
Mg3,40722560
Fe0,18127<0,001
Cu0,27690,08
Zn0,2214186
Ca0,35103396
Si0,02300,24
Cr0,01of 1.340,65
Al0,241236,05

These example results show that the Nickel concentration in the eluate was about 60 g/l, which, in the opinion of the authors, approximately 60% greater than the capacity of saturation is rich in resin. It is also noted that most of the impurities, such as magnesium and manganese, was the waste solution produced through the output 3, and, as a result, the concentrated eluate suitable for electrolytic izvlechennaya.

EXAMPLE 3

This example illustrates the desorption of copper from a saturated resin, which is pre-saturated during sorption extraction of copper from liquid heap leaching. Copper concentration was 2 to 6 g/L.

Saturated capacity of the resin used in this copper test was 55-64 g/L. During this test, the resin flowed through desorption column with a flow rate of approximately 100 ml/h

Desorption the experiment was carried out in 750 ml borosilicate glass column corresponding to the apparatus shown in Fig.6. U-shaped colon was fully insulated to maintain the temperature in the column 60-70°C.

10% solution of sulfuric acid used as desorbent, which was preliminarily heated to 60-70°using an electric heater, inlet 4 Stripping solution. The flow desorbent supported at a speed of about 75 ml/h

Additionally, after the deposition of copper sulphate, was pumped into the pre-heated mother liquor in the middle of the chamber 1 through the inlet tube 12 with a capacity of about 85 ml/h In the mother solution, the concentration of copper was about 45 g/L.

The flow of the impurities were removed from the chamber 2 through the flow 3 flow ˜60 ml/h, and the concentration of copper was less than 100 hours/million This solution containing impurities, can be reused in the way heap you is aleciane copper.

The saturated flow of the eluate were collected from the bottom of the apparatus through the pipe 8 and the control valve 15 with a flow rate of 100 ml/h with a copper concentration of about 100 g/l and a temperature of ˜65°C.

The flow of the eluate was cooled to 20°With continuous stirring and approximately 234 g of crystals of copper sulphate besieged from each liter flow of the eluate. After filtration of the crystals of copper sulphate mother liquor with a concentration of copper of about 45 g/l was heated to ˜70°and re-used with the flow in the inlet pipe 12.

EXAMPLE 4

This example illustrates the desorption of molybdenum from a saturated resin, which was filled during the adsorption of molybdenum-containing solutions. The concentration of molybdenum in these solutions was ˜1 g/l, therefore the equilibrium saturated capacity of the resin was about 100 g/l

Desorption the experiment was carried out in 30 l of the column corresponding to the apparatus shown in figure 1. Saturated resin was applied to the external chamber 2 of the column through the tube 5. During this experience supported the flow of resin ˜3 l/h

10% ammonia solution is used as desorbent. This solution was pumped into the inner chamber 1 of the column through a tube 4 with the valve 14 in the open position. Speed supported 4 l/h

The flow of the waste solution with a concentration of molybdenum is less than 200 hours/million was collected from the drain 3 with a flow rate of about 2 l/h and return the Ali-rich solution through sorption.

The saturated flow of the eluate were collected from the bottom of the column through the lattice filter 11 and the pipe 8. The amount of the eluate was controlled by means of valve 15. The concentration of molybdenum in the flow of the eluate was ˜150 g/l, and concentrations of major impurities were insignificant. This solution is suitable for economical extraction of chemically pure paramolybdate ammonium.

EXAMPLE 5

This example illustrates the method of Stripping Nickel from a saturated resin with a capacity of saturation of Nickel of about 42 g/l Resin saturated during the sorption of Nickel from sludge atmospheric leaching of laterite.

Desorption equipment consisted of 750 ml columns in accordance with the embodiment shown in figure 3. Saturated resin was applied to the column through the tube 5. The flow of the resin during this experience was maintained equal to ˜100 ml/h

10% solution of sulfuric acid was used as Stripping solution. Consumption of desorbent regulated by a peristaltic pump and was maintained equal to ˜75 ml/hour Desorbent pumped in the upper part of the desorption zone of the column through pipe 4 and the valve 14.

The solution after the electrolytic method of extraction of Nickel containing 43 g/l, was applied in the middle of the desorption zone of the column with a flow rate of ˜85 ml/h through the tube 12.

The flow of waste solution (60 ml/h) was removed from the colon the s through the drain 3. This solution contains about 200 hours per million of Nickel and can be reused in the method of leaching.

The flow of the eluate were collected from the bottom of the column through a valve 15 and a pipe 8 with a flow rate of about 100 ml/h, and contained about 85 g/l of Nickel. This solution can be used for the electrolytic extraction of Nickel.

1. Apparatus for desorption of the compounds from the ion-exchange resin having adsorbed therein impurities and target material, and the apparatus includes first and second chambers, which are arranged so that when the resin is fed to the first camera, and it moves from the first chamber into the second chamber, and deformirujuschij solution serves the second chamber, and is moved from the second chamber into the first chamber such that (i) impurities having a lower affinity for the resin than the target material, can decorrelates from the resin, and the target material may absorb the resin from Stripping solution in the first chamber and, thus, conditions are created when the flow of impurities having a high impurity concentration and a relatively low concentration of the target material, can be produced from the first chamber through the first output and (ii) the target material can decorrelates from the resin in the second chamber, and to create conditions where rich stream having a low impurity concentration and a relatively high concentration of the spruce material, can be produced from the lower parts of the first and/or second chambers through the second output.

2. The apparatus according to claim 1, where the resin is moving down in the first chamber and up the second camera, and deformirujuschij solution moves in countercurrent to the direction of resin in the above-mentioned cameras.

3. The apparatus according to claim 1 or 2, in which the flow of impurities is withdrawn from the upper part of the first chamber.

4. The apparatus according to claim 1 or 2, in which the first and second chambers are connected through flow connection in such a way that deformirujuschij solution can flow under gravity from the second chamber into the first chamber.

5. Apparatus for Stripping material from a saturated ion exchange resins, and the apparatus includes first and second chambers, which are arranged so that when the resin may move down in the first chamber and up the second camera, and deformirujuschij solution can flow in countercurrent to the resin, the first and second inputs for supplying saturated resin into the first chamber and the Stripping solution into the second chamber, respectively, and first and second outputs for release of fluid from the apparatus, and a third outlet for release of desorbed resin from the second chamber; means providing for the transfer of resin from the first chamber the second chamber and moving the resin up in the second chamber; whereby the first stream Stripping solution provided is relatively high impurity concentration and a low concentration of the target material, can release from the first output, the second thread Stripping solution containing a relatively high concentration of the target material and a low concentration of impurities, can release from the lower parts of the first and second chambers and/or away from the Stripping solution passing from the second chamber into the first chamber from the second output, and desorbed resin can release from the third output of the second camera.

6. The apparatus according to claim 5, in which the first and second chambers are located and associated flow connection in such a way that the pressure of the liquid Stripping solution in the second chamber causes deformirujuschij solution to flow upwards in the first chamber.

7. The apparatus according to claim 5, in which the first outlet for releasing the first stream is placed in the upper part of the first chamber.

8. The apparatus according to claim 5, in which the third exit for the release of desorbed resin is placed in the upper part of the second chamber.

9. The apparatus according to claim 5, in which the third exit to move desorbed resin from the first chamber is connected with the intermediate chamber, which may be collected desorbed resin.

10. The apparatus according to claim 5, which further includes control means for controlling the speed of removal of the resin from the second chamber.

11. The apparatus of claim 10, in which the control means measures the liquid level Stripping of rest the RA in the first chamber to regulate the speed, with which the resin is removed from the second chamber.

12. The apparatus according to claim 5, in which the desorption of impurities from the resin occurs in the upper zone of the first chamber and, thus, allows the target material in desorbers solution absorb on the resin in the upper zone.

13. The apparatus according to claim 5, in which the desorption of the target material occurs in the upper zone of the second chamber.

14. The apparatus according to claim 5, in which the second chamber has a different input solution, which when filing will increase the concentration of the target material in the second chamber and, thus, to reduce the impurity concentration in the second stream.

15. The apparatus according to claim 5, in which the first and second chambers connected by the flow, adapted to move the resin and Stripping solution between cameras.

16. The apparatus according to claim 5, in which the first and second chambers are connected in a U-shaped configuration, where the first and second chambers form the shoulders of the U-shaped base provides the flow.

17. The apparatus according to clause 15 or 16, in which the second thread Stripping solution containing a high concentration of desorbed material, can release from duct located between the first and second chambers.

18. The apparatus according to claim 5, in which the first and the second camera is positioned so that one of the cameras is inside another camera.

19. The apparatus according to p, in which the second chamber of the races is oleaut concentrically in the first chamber so that the first chamber has an annular cross-section.

20. The apparatus according to claim 19, in which the second chamber is open down the hole, through which deformirujuschij solution in the second chamber can flow directly from the second chamber into the first chamber, and resin from the first camera can move through that hole up in the second chamber.

21. The apparatus according to claim 20, in which the second stream is released from the first chamber into the lower holes of the second camera.

22. The way desorption of substances from the ion-exchange resin having adsorbed impurities in it and the target material, and the method includes processing the ion exchange resin in the apparatus having first and second chambers, where the method includes the stage

a) desorption of impurities from the resin in the first chamber desorbers solution, so that the target material has a greater affinity for the resin than the impurities, can absorb on the resin from the Stripping solution and, thus, creating conditions when a thread having a high impurity concentration and a low concentration of the target material can be released from the first chamber; and (b) desorption of the target materials from the resin treated according to stage a), the second camera desorbers solution and, thus, creating conditions when the stream having a high concentration of the target material and the low concentration of the Sabbath.tion of impurities, can be released from the device.

23. Method for desorption of the compounds from the resin in the apparatus having first and second chambers, United running connection, and the method includes the stages of (a) the filing of a saturated resin containing adsorbed on her target materials and impurities into the first chamber, and movement of resin down in it; (b) the movement of resin from the first chamber into the second chamber and movement of the resin up in it; (c) the filing of Stripping solution into the second chamber so that the solution flows down the second chamber and up into the first chamber in countercurrent to the resin; (d) release of desorbed resin from the second chamber; (e) the release of the first thread Stripping solution containing a high impurity concentration and a low concentration of the target substance from the first chamber; and (f) release the second thread Stripping solution containing a relatively high concentration of the target material and the relatively low concentration of impurities from the bottom of the first and/or second chambers, and/or from a solution, the current between the cameras.

24. The method according to item 23, in which any two or more of the steps from a) to f) are carried out simultaneously.

25. The method according to item 23 or 24, in which impurities having a lower affinity for the resin than the target materials, desorbers from the resin, and the target material can absorb on the resin in the first chamber.

26. The method according to item 23, which on the sorption of impurities from the resin, essentially, occurs in the upper zone of the first chamber and, thus, allows an additional target material from the Stripping solution absorb on the resin in the upper zone of the first chamber.

27. The method according to p, in which the first stream is produced at stage (e), produced from the upper zone of the first chamber.

28. The method according to item 23, in which the target materials desorbed from the resin, increase the density of the Stripping solution and, thus, cause a high concentration of the Stripping solution to settle towards the lower areas of the first and second chambers.

29. The method according to item 23, in which the rate at which resin produced in stage (d), adjust the level of the liquid in the first chamber.

30. The method according to item 23, in which the resin, produced by stage (d), produced from the upper zone of the second chamber.

31. The method according to item 23, which includes a step of feeding a solution containing a target substance, a second chamber and, thus, decreasing the impurity concentration in the second chamber.

32. The method according to p, in which the temperature of the concentrated solution vary from approximately 60 to 100°C.

33. The method according to p, in which the solution containing the target material, serves the second chamber in the space between the upper and lower zones of the second camera.

34. The method according to item 23, in which the movement of the resin up the second camera according to the article the Hai b) includes the use of technology ripple resin.

35. The method according to item 23, in which deformirujuschij solution flows upward in the first chamber according to the stage) as a result of the pressure of the fluid in the second chamber.

36. The method according to item 23, in which the first and second chambers are connected in a U-shaped configuration, where the first and second chambers form the shoulders of the U-shaped base provides the flow through which can be moved resin and deformirujuschij solution.

37. The method according to p, in which the second thread Stripping solution containing a high concentration of the target material, can release from duct located between the first and second chambers.

38. The method according to item 23, in which the first and second camera feature so that one camera is placed inside another camera.

39. The method according to 38, in which the second camera is fitted concentrically within the first chamber so that the first chamber has an annular cross-section.

40. The method according to 39, in which the second chamber is open down the hole, whereby deformirujuschij solution in the second chamber can flow directly from the second chamber into the first chamber, and resin from the first camera can move through the hole up to the second camera.

41. The method according to p, in which the second stream is released from the first chamber into the lower holes of the second camera.



 

Same patents:
The invention relates to the field of metallurgy, namely the recovery of noble metals and platinum group metals from the poor and ultrametric industrial waste

The invention relates to a process for recovering molybdenum from aqueous solutions of tungstate and can be used in ferrous and nonferrous metallurgy, as well as treatment of industrial and domestic wastewater
The invention relates to a method for producing tungsten and/or molybdenum-containing solution from the alkaline solution of the opening of the respective raw materials

The invention relates to hydrometallurgy, in particular coal sorption technology for the recovery of precious metals from solutions and slurries

The invention relates to methods of regeneration of the anion exchange resin saturated with noble metals

FIELD: technological processes.

SUBSTANCE: invention pertains to methods of cleaning cationite filters from products of regeneration and iron compounds and is designed for use in an iron exchange system of water treating works, heat power engineering, public service boilers, as well as industries which use treated water in their technological processes. The method involves passing water from top to bottom through the cationite, with hardness of not less than 2.5 mg-eq/l as calcium, speed of 6-8 m/h and flow of water to residual hardness of 0.03 mg-eq/l as calcium, in the washing water. Cleaning is done with specific flow of not more than 3 m3/m3 of cationite in two stages. On the first stage, initial water is passed through the cationite, treated by a magnetic field to residual hardness of 0.7 mg-eq/l as calcium, in the washing water. The cationite is then cleaned in stagnant magnetic water for 1-2 hours. On the second cleaning stage, initial water is passed through the cationite without magnetic treatment. Magnetic treatment is done by passing initial water at a speed of 0.5-1.5 m/s through a pipe shaped magnetic device, based on permanent magnets with flux density of 0.2-0.35 tesla. The invention provides for increasing economical efficiency of the method and lowering ecological damage by reducing specific flow of cleaning water, increasing the working exchange capacity of the cationite due to increased speed and degree of cleaning from products of regeneration and iron compounds.

EFFECT: increased economical efficiency of the method of cleaning cationite filters from products of regeneration and reduced ecological damage.

2 cl, 3 dwg, 3 tbl, 2 ex

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to regeneration of basic anionite catalysts for process of production of alkylene glycols via hydration of corresponding alkylene oxides. Method according to invention consists in treatment of spent catalyst with aqueous solution of inorganic salts of iodine and inorganic acids or with hydroiodic acid aqueous solution.

EFFECT: achieved complete restoration of initial volume and selectivity of catalyst and thereby prolonged lifetime of expensive anionite catalyst.

1 tbl, 8 ex

FIELD: water treatment.

SUBSTANCE: invention is dealing with separation of cationite/anionite mixture utilized in multifunctional filters in deep water treating systems to be further regenerated. Method is based on difference in densities of the two ionites and employs composition constituted by fluorine-containing saturated acyclic hydrocarbon or fluorine-containing ether, which have densities within a range of 1.30-1.90 kg/dm3, and saturated acyclic hydrocarbon of general formula CnH2n+2 (n=6-9) having density between 0.65 and 0.8 kg/dm3.

EFFECT: preserved ion-exchange capacity of resins before regeneration.

2 ex

FIELD: distillery industry; soft drink industry; other industries; methods of purification of the washing alkaline solutions of the bottle washing machines.

SUBSTANCE: the invention is pertaining to the methods of purification of the washing alkaline solution of the bottle washing machines from the suspended particles, the carbonates, the aluminates and other impurities introduced in it at washing of the reusable bottles. The method provides for batching into the polluted washing solution of the spent regeneration solutions (SRS) of the ion-exchange Na-cationite screens or N-cationite screens containing the calcium chloride and the magnesium chloride with the subsequent clarification of the liquid. The volume of the batched reclaim is accepted of not less than 3 % from the volume of the purified washing solution. The method of the invention allows to raise duration of usage of the washing alkaline solution without deterioration of its washing characteristics, to restore the chloride-containing reclaims, and also to diminish the discharge of the pollutants and to reduce expenditures on buying of the chemical reactants for purification of the washing alkaline solution. The settlings and the tailings formed at purification of the washing solution are subjected to dehydration and utilization.

EFFECT: the invention allows to raise duration of usage of the washing alkaline solution without deterioration of its washing characteristics, to restore the chloride-containing reclaims, to diminish the discharge of the pollutants, to reduce expenditures on buying of the chemical reactants for purification of the washing alkaline solution, to dehydrate and utilize the settlings and the tailings formed at purification of the washing solution.

2 cl, 2 ex, 2 tbl

FIELD: water purification and preparation by means of filtering modules containing ion-exchange resins for softening of water.

SUBSTANCE: proposed method consists in passing water to be cleaned through layer of floating inert material and ion-exchange resin in downward direction and regeneration of ion-exchange resin by pressing its layer by liquid medium flow in upward direction, passing of regenerating solution, gravity sedimentation of resin and washing-off residues of regenerating solution. Filtration is performed through at least two filters mounted in succession; charge of ion-exchange resin is so selected that volume of resin in first filter is no more than 40% of total amount of resin used for cleaning; at regeneration, resin is so pressed that it passes through stage of formation of fluidized layer. In pressing the resin during raising it, rate of flow in first filter shall be below rate of flow required for piston-like raising of resin by at least 25%. Liquid is delivered to first filter in pulse mode or raising of resin is carried out simultaneously with bubbling of gas through it.

EFFECT: enhanced efficiency; reduced consumption of salt for regeneration and water.

6 cl, 1 tbl, 4 ex

FIELD: chemical industry; other industries; methods and devices for modification or reregeneration of zeolites.

SUBSTANCE: the invention is pertaining to the methods and devices for modification or reregeneration of zeolites concerning the group of the ion-exchangers - cationites. The method provides, that the bosh is divided into two chambers by the partition having the properties of the fine filter of the water. The electrodes are introduced into the chambers. One of the chambers is loaded with the zeolites. The bosh is filled with the water. The chamber with zeolites is loaded with the salts, which cations are used for modification and regeneration of the zeolites in the quantities, which are necessary and sufficient for formation in the water of the concentration of these salts of 1 - 10 %. Then the direct current voltage of 5-35 V is fed to the electrodes: the negative voltage is fed to the electrode in the chamber with the zeolites, and the positive voltage is fed to other electrode, switch on the device used for the zeolites washing, wash the zeolites in the bosh with the water solutions of salts within 3-10 hours. The invention presents the device for realization of the method. The technical result of the invention is the increased intensity of the ion exchange process in zeolites, the reduced duration of the process, the decreased amount of the salts consumption for regeneration.

EFFECT: the invention ensures the increased intensity of the ion exchange processes in zeolites, the reduced duration of this process, the decreased amount of the salts consumption for regeneration.

2 cl, 1 dwg

FIELD: plant growing.

SUBSTANCE: method for reducing of hydroponic substrate of natrolite and vermiculite involves washing substrate with water; preparing aqueous suspension of washed out substrate; providing bubbling thereof with air; performing supersonic processing; removing by means of water; washing substrate; drying and processing in electric field of 300-350 kV/m intensity.

EFFECT: intensified substrate reduction process.

1 ex

FIELD: restoration of exchange properties of ionites; chemical and pharmacological industries; chemical engineering; treatment of drinking water and service water at low hardness; ecological processes of cleaning waste water from cations and anions of toxic dissolved agents.

SUBSTANCE: proposed method includes simultaneous treatment of material in DC field of high-frequency generator, continuous supply of water through layers of ion-exchange material located between electrodes; one of them performs function of anode; it is connected with high-frequency generator output; treatment of ion-exchange material is performed at constant DC magnitude equal to (0.1-12) V and frequency of AC fluctuations equal to (6.5-7.3)MHz at respective resonance frequency of water ion oscillation; cathode is connected with second output of high-frequency generator.

EFFECT: reduced power requirements; facilitated procedure of ionite regeneration due to treatment of ion-exchange material at constant DC voltage and AC fluctuations.

1 dwg, 1 tbl

FIELD: water treatment.

SUBSTANCE: invention relates to regeneration of cationites used on water-softening plants. In this process, of low-acid carboxylic cationites are converted into their H-Na form by consecutively passing (i) acid in stoichiometric proportion until pH 3.9-4.3 is achieved and (ii) 1.0-1.5% sodium chloride solution through cationite layer.

EFFECT: reduced consumption of reagent for the same degree of transformation.

4 tbl, 3 ex

FIELD: waste water treatment.

SUBSTANCE: invention relates to treatment of waste waters originated from fluorine-containing polymer production. Fluorine-containing emulsifiers, in particular perfluorooctanoic acid, are bound by anion-exchange resins. Further, indicated emulsifiers are washed out from anionite with water-organic mixture containing some amount of ammonia and having boiling temperature below 150°C. Ammonia-containing solvent is preferably distilled away and emulsifier and ammonia-containing solvent are reused.

EFFECT: increased concentration of emulsifier in eluate.

5 cl, 4 tbl, 5 ex

FIELD: chemical industry; nonferrous metallurgy; other industries; production of the apparatuses for purification of the waste waters by ion exchange.

SUBSTANCE: the invention is pertaining to the apparatuses for purification of the waste waters by ion exchange. The apparatuses may be used in the galvanic and chemical production for purification of the waste waters and the production process liquids. The column counter-current ion-exchange filter contains the cylindrical housing with the inlet and outlet windows used for delivery and withdrawal of the ion-exchange filtering material, the upper and lower bottoms, the unions of the fed treated water and withdrawal of the purified water, the main pipes for feeding of the fresh ion-exchange filtering material and withdrawal of the spent ion exchanger. Inside the housing there is the rotor with the mounted on it feed screw. The feed screw is formed by the double-threaded perforated non-falling partitions and having on its external diameter the perforated non-falling jacket. In the jacket at the level of the inlet and outlet windows of the housing there are the windows used for delivery and withdrawal of the ion-exchange charge. In one apparatus the continuous process of purification of the contaminated water takes place in the presence of the anion-exchanging and cation-exchanging absorbers at the continuous change of the ion-exchanger. The technical result of the invention is the increased productivity of the ion-exchange filter and the reduced cost of the purification.

EFFECT: the invention ensures the increased productivity of the column counter-current ion-exchange filter and the reduced cost of the purification.

3 cl, 2 dwg

The invention relates to equipment for ion-exchange processes and can be used in chemical, hydrometallurgical and other industries

The invention relates to a hardware design process in a heterogeneous system, liquid - solid, such as sorption, leaching, dissolution

The invention relates to apparatus for the implementation of a counter-current mass transfer between granular and liquid phases with subsequent separation of the solid and liquid phases and transport prepared a certain portion of the granular phase for the next stage of the process and can be used in the chemical and related industries
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