Experimental conditions of chromatographic nitrogen isotope separation with different migration distance
Enriched stable isotopes of many elements have been widely used in many aspects and such isotopes have been primarily used as the tracer for agricultural and biochemical studies and the availability of the isotopically labeled compounds have been now extensively increasing. Chemical exchange separation of isotopes is based on the equilibrium fractionation of isotopes between two phases, ion exchange isotope separation which is one of the chemical exchange methods, is based on the chemical equilibrium between a stationary phase and a mobile fluid phase. Displacement always results in a sharp boundary between the bands of eluted solute and displacing solute in this method. Displacement chromatographic ion exchange technology for isotope separation is described in this chapter. This chapter mainly divided into two sections. Ion exchange system, ion exchange separation and analysis are introduced in the former section as the basic theory and concept for ion exchange separation. The second section is about the experiment parts of nitrogen isotope separation which include nitrogen isotope application, nitrogen isotope separation process, nitrogen isotopic analysis with mass spectrometry and the obtained results and discussion which were performed by our recent experiments.
2. Ion exchange system
Enriched stable isotopes of many elements have been widely used in agriculture, medicine, biochemistry and industry, especially in nuclear industry. Such isotopes have been primarily used as the tracer for agricultural and biochemical studies and the availability of the isotopically labeled compounds have been now extensively increasing. In order to meet the demand, the need of developing a practical cost-effective process has been enlarged. The most heavy stable isotopes are produced in relatively small quantities, many light isotopes are used in large quantities. Distillation is used in industry to separation the isotopes of hydrogen, carbon, boron, nitrogen and oxygen. Chemical exchange is the satisfactory technique for separating isotopes of light elements because of their relatively high simple process factors (separation factors).
Chemical exchange separation of isotopes is based on the equilibrium fractionation of isotopes between two phases, i.e. one of the isotopes is concentrated more abundantly in one of the phases than in the other phase if two chemical species are distributed in each phase. In this method, the enrichment of the isotopes concerned is achieved when the simple process of isotope separation is multiplied, by arranging the countercurrent contacting of two substances. The countercurrent contacting of the two different chemical substances is most easily realized in vapor-liquid or liquid-liquid system. The contacting takes place in conventional systems such as packed columns, mixer-settlers, etc. In this process it is necessary to provide reflux at the product end of a chemical exchange plant; the end which the desired isotope being enriched. In general, chemical refluxing is used to complete the conversion of one chemical species into the other at the end of the multi-stage contactor system.
Ion exchange isotope separation, which is one of the chemical exchange methods, is based on the chemical equilibrium between a stationary phase and a mobile fluid phase. In the past, many researchers have studied isotope fractionation on the isotopes both for light and heavy elements in this liquid solid system[1-5] and several isotopes especially for nitrogen isotope have been successfully enriched in laboratory scale by using displacement chromatographic technique [6, 7]. In this process a band of adsorbate is eluted through the column by a displacing solution, which the rate of movement of the band is determined by the equilibrium between solution and adsorbent, not of the material of the band but of the displacing adsorbate. Displacement always results in a sharp boundary between the bands of eluted solution and displacing solution. Thus, the adsorption band moves with keeping a constant band length. During the migration the isotopes in the band are rearranged in order of the distribution coefficients.
3. Ion exchange separation and analysis
3.1. Ion exchange column
3.1.1. Batch and column operation
Ion exchanges are generally employed in the two different modes of operations: batch and column operation. The batchwise operation consists of contacting the whole of an electrolyte solution to be treated with a mass of exchanger and then separating the two phases by means of filtration, decantation, etc. It is quite obvious that for those exchange reactions that do not approach completion, a batchwise operation must be repeated many times before complete transformation is realized. The more unfavorable the equilibrium, the larger the number of stages are necessary for a given degree of exchange or separation.
The operation of an ion-exchange reaction by leaching the exchanger in a columnwise manner achieves most efficiency the same goal that would take many stepwise stages in a batch method. The column operation is essentially an elaborate multiple batchwise technique in which the uppermost portion of the column is constantly contacting fresh electrolyte whereas the lower portions contact the electrolyte not adsorbed by the upper exchanger. This procedure permits the exchanger bed to become fully exhausted at the top and then gradually downward. Ion exchange chromatography is a technique in which resolution of a mixture is achieved by virtue of differences in migration rates of the components in a column packed with an ion exchanger.
3.1.2. Chromatographic column operation
Chromatography was first applied to colored substances where “bands” of different colors can be seen while they move down the column. The chromatographic column operations are generally conducted in the manners of elution development, displacement development, and frontal analysis [8-10]. In the development techniques, a certain amount of the mixture is introduced at the top of the column and is then “developed” or “eluted” by a suitable agent. In frontal analysis, the mixture is continuously fed to the column. The front boundaries of the various components emerge at different times due to the differences in the migration rates.
3.1.3. Preparation of ion exchange column
In the analytical applications of ion exchange, it is necessary to utilize uniform particle size ion exchangers in order to avoid irregular flow due to the distribution of particle size. For this purpose, the wet resins in the form of H+ were screened prior to the packing. The stainless steel screens of 42, 80, 200 and 400 meshes are used commonly. Then the ion exchanger with water in a beaker was stirred, and poured the slurry of resin into the column.
Under no circumstances must bubble or air be allowed to form in the bed of the ion exchanger beads. In operation, therefore, the bed must never be allowed to drain; the liquid level must not fall below the top of the bed. The water level was kept at 1-2 cm above the top of the bed during the operation.
The fresh ion exchanger provided by the supplier usually contains impurities, such as low molecular weight organic substances, and metallic ions, such as ferric ions. The new ion exchanger bed was, thus, washed in order to remove these impurities and metallic ions by following manner:
The bed is first washed with a ten fold column volume of 2.0 M hydrochloric acid.
The same amount of 10 M sodium chloride is then fed into the column.
Repeat the process (1) and (2) for three times.
Repeat the process (1).
The bed is finally rinsed with distilled water until no leakage of H+ is recognized.
In the ion exchange chromatography, high pressure resistant pyrex glass columns with a water jacket were used in the studies of isotope separation. The column of which the inside diameters of 8, 10 and 20 mm were prepared so that the operations are able to be conducted up to the column pressure of 50, 30 and 20 kg/cm2 in each column. To feed solutions, the microprocessor controlled, double plunger type titanium high pressurized pumps were used. The Teflon tubing of 1.0 mm i.d. was employed to connect column and pump. To monitor the column pressure, a pressure gauge with a safety device was placed between the column and the pump. In addition, an air damper was used in order to prevent the piston flow, especially at high flow rate runs, when loading solutions into columns. A schematic diagram of the apparatus used for the ion exchange separation is shown in Figure 1. Water jacket was employed to remove the heat of reaction and maintain the column temperature throughout the experiments by circulation the thermostated water.
4. Nitrogen isotope application
Enriched isotope of 15N has been a very valuable commercial product for which there is presently a growing demand in various scientific research and industry applications. In the agricultural field, 15N has been extensively used to study nitrogen cycling in soil-plant relationships. The fertilizer efficiency, distribution, assimilation and metabolic plants in the plant, symbiotic nitrogen fixation and the behavior of fertilizer in soils have been studied with use of 15N. Adriana et al. evaluated the nitrogen fixing capacity of a range of commercial cultivars of maize (
4.1. Nitrogen isotope separation process
The separation of the nitrogen isotope has been studied since Urey et al. first succeeded in concentration of the nitrogen isotope of atomic weight 15 by using chemical exchange between ammonia gas and aqueous solutions of ammonium salts . In their work, the considerable quantities of material containing up to 75% atom of 15N was obtained by exchange between ammonia and aqueous ammonium nitrate solutions. Later, in 1955, Spinder and Taylor  developed the chemical exchange method involving the exchange between nitric acid and nitric oxide as Equation 1:
The fractionation factor of the exchange reaction obtained at 1.0 M nitric acid 1.062 is extremely favorable compared with the separation factors of most other possible separation methods of nitrogen isotopes by chemical system. In this process, the 15N concentrates in the nitric acid and thus 15N enriches in the lower part of the exchange column. In Japan, 15N has been commercially produced using this technique, which is called NITROX process. In Romania, Axente et al. have studied this process for thirty years using a laboratory-scale experimental plant . Some other isotope separation methods such as distillation and thermal diffusion have also proved to be satisfactory for 15N separation [24-27].
Ion exchange process on nitrogen isotope separation has been studied since Spedding et al. first succeeded in the enrichment of 15N by cation exchange chromatography . In their experiment, the separation factor of the isotopic exchange between the two phases of the dilute ammonium hydroxide solution and the cation exchange resin (Dowex 50-x12) in ammonium form was measured as 1.0257±0.0002. A few years later, the studies on the nitrogen isotope separation by ion exchange were reported by two Japanese research groups Ishimori and Kakihana . Ishimori investigated the influence of operating temperature and concentration of ammonium solution on the isotope effects in a batch equilibrium system. Kakihana measured the separation factors of nitrogen isotopes for NH3 and NH4Cl in acetone water and ethanol water mixture systems. Afterwards, in 1980s, Park and Michaels studied the separation process developed by Spedding et al. under various operating conditions using columns packed with sulfonated polystyrene-divinylbenzene copolymers . In the recent years, Krugrov et al. studied NH3-NH4+ system using SMB (simulated moving bed) process for various flow rates under total reflux  and the theoretical analysis of separating nitrogen isotopes by ion exchange was reported by Aoki et al .
4.2. Nitrogen isotopic analysis with mass spectrometry
If an aqueous solution of ammonium hydroxide is placed in contact with a cation exchanger, the following exchange reaction occurs:
the result of which, under equilibrium conditions, is that the heavy nitrogen isotope, by means of the ammonium ion, is distributed more abundantly in the solid phase, which is the cation exchanger. In order to multiply the elementary effect for separating 15N, the following chromatographic separation process developed by Spedding was employed : the ion exchanger bed was first converted to the hydrogen form by passing 2.0 M hydrochloric acid through the column until the bed was saturated. The bed was then rinsed with distilled water and an ammonium hydroxide solution of certain concentration was added. At the lower end of an ammonium band, the following reaction takes place:
Where -R denotes the fixed anion of cation exchanger. Since the equilibrium constant of this exchange reaction is on the order of 109, the reaction is far to the right, resulting in an extremely sharp boundary. The ammonium ion comes to chemical equilibrium within the system very rapidly and isotopic equilibrium tends to be approached as the solution passes over the cation exchanger. In the frontal analysis, the effluent is collected in fractions at the bottom of the column when the ammonia solution of which the front part of the ammonium band is emerged. Prior to the collection, certain volumes of hydrochloric acid are initially added in the sampling tubes to prevent the ammonia from degassing. Since the 15N isotope is depleted in the front of the band, 14N isotope is enriched in the effluent.
In the displacement band chromatographic process, an ammonia solution is fed into the column until an ammonium adsorption band of the desired length is formed. The concentration of the fed ammonia solution was adjusted approximately at the concentration of the eluent in each operation. A caustic solution (NaOH or LiOH) was then fed into the column to elute the ammonium band in the reverse breakthrough manner. At the top of the ammonium band, the following reaction takes place:
which, having an equilibrium constant of about 105, in turn guarantees a very sharp boundary at the rear end of the band. The ammonium ions are continuously released from the cation exchanger and converted to ammonium hydroxide by an equivalent of sodium (or lithium) ions which will be deposited at the rear edge of the band. The ammonium hydroxide solution moves down along the band until it reaches the front edge of the band. The diagram of the displacement band chromatographic process for separating nitrogen isotopes with the use of a cation exchanger is shown in Figure 2. The countercurrent movement of NH3-NH4+ ions in two phases develops a longitudinal isotopic distribution profile within the band. The 15N isotope is enriched in the rear end of the band. The effluent of the rear part of the band was collected in fractions at the bottom of the column.
The volume of the fraction was determined by gravimetry, measuring the weight of the sample solution. The concentrations of ammonium and sodium (lithium) ions in the fractions were determined by an ion chromatography analyzer. The collected samples in the form of ammonium chloride were converted to nitrogen gas by adding a solution of potassium hypobromide(KBrO). The reaction involved is as follows:
The solution of potassium hypobromide was prepared by following process:
Add 36.5 g of sodium hydroxide and 2.2 g of potassium iodide into 170 g of distilled water.
Cool the solution 1) by ice and then 25 g of bromine is added with agitation.
The yellow colored solution obtained is left standing in a refrigerator for overnight.
The KBrO solution was stored in a refrigerator since potassium hypobromide is easily decomposed to potassium bromide and oxygen in light or by elevation of temperature. The Rittenberg was employed in order to prepare nitrogen gas samples for isotopic analysis and the apparatus of the nitrogen conversion system is shown in Figure 3. The preparation procedure of nitrogen gas samples is described below:
Put a certain volume of ammonium chloride sample (0.1-1.0 cm3) in one side and a stoichiometrically excess amount of potassium hypobromide in the other side of a Rittenberg glass tube A.
A cold trap D is cooled with liquid nitrogen to prevent contamination of water in the vacuum system during evacuation.
Freeze the solutions in the Rittenberg galss tube with liquid nitrogen.
Open the glass stopcocks B and C which are used to control the vacuum manipulations to pump out the air by an oil rotary pump. After the evacuation, the stopcock B is closed.
The liquid nitrogen vessel is then removed from the Rittenberg tube to admit the solutions to be melted.
Freeze the solutions again and open the stopcock B so that the gas generated during the melting is evacuated.
After the evacuation, both stopcocks B and C are closed and Rittenberg tube is taken off from the conversion system.
Finally, nitrogen gas is obtained by mixing the solutions of ammonium chloride sample and potassium hypobromide in the Rittenberg tube.
The nitrogen gas sample is then introduced to the mass spectrometer for the isotopic analysis.
5. The effect of migration distance to the nitrogen isotope separation
The sulfuric strong acid cation exchange resin SQS-6(high porous type, cross linking 8%, particle size 60-90 um in the form of NH4+, provided by Asahi Chemical Industry Co., Japan) was packed uniformly in a pressurized glass column with a water jacket. The microscope view of H+ type SQS-6 resin was shown in Figure 4. The ion exchange resin in the column preliminarily conditioned to the H+ form with 2.0 M HCl solution, then pure water was feed into the top of the column to remove the free H+ in the resins. 0.2M NH4OH solution was feeded into the column to form 1.0 m ammonium adsorption band and the band was eluted by the displacing solution of 0.2M NaOH in the reverse break-through manner. The flow rate and band velocity were controlled by feeding pump and the column pressure was monitored by high pressure pump. The temperature of the column was kept constant throughout the experiments by passing the thermostated water through the water jacket. The effluent, which emerged from the column, was collected using a fraction collector. In order to prevent the NH4OH samples from de-gassing, certain volumes of excess HCl solutions were added in the collection tubes prior to the samplings. Considering the long migration distance for the purpose of large scale production, it is necessary to regeneration column after the ammonium adsorption band pass through certain column. When the rear boundary of ammonium adsorption band enter into the next column, the first column was separated from the connection system and eluted by 2.0M HCl for regeneration, the rinse volume was at least five times larger than that of the resin’s volume. The concentrations of NH4+ in the fractions were determined by ion chromatography analyzer and the mass peaks of 14N15N and 14N14N of the samples were measured with the mass spectrometer and the isotopic abundance of 15N was calculated from the ratio of the peak height.
The separation of nitrogen isotopes by means of ion exchange resin is based on the isotopic fraction between ammonia in aqueous solution and ammonium ion in the ion-exchange resin as shown in the Equation 6. The single stage separation factor α or the separation coefficient ε is defined by:
Where denotes the concentration of isotopes in the aqueous phase and the concentration of the isotopes in the resin phase.
In order to evaluate the chromatographic efficiency of nitrogen isotope enrichment, HETP (height equivalent to a theoretical plate) is introduced. HETP is usually calculated using the slope of the isotopic distribution curve in the steady-state of isotope separation after migration and is calculated by the following Equation 7:
Where H is the HETP and L is the migration length. The slope k is experimentally determined by using the following Equation 8:
Where r is the isotopic ratio of nitrogen sample and ro is the isotope ratio of feeding material. The term (L-x) is the distance between inner band location x and the rear or front boundary of which the migration length is L. Equation 8 indicates that plotting ln(r-ro) against (L-x) for the experimental data produces a linear line with the slope of k.
Nitrogen isotope separations with different migration distance were performed and the experimental conditions were mentioned in Table 1.
|Run||Migration distance (m)||Column φ (mm)||Eluent NaOH Conc.(M)||Flow rate (cm3/min)||Band velocity (m/d)|
The chromatographic elution curve for Run 4 as an example is given in Figure 5. It is seen that ideal displacement chromatograms are obtained and a sharp band boundary between the ammonium band and sodium band is maintained during the long migration at the current experimental conditions. The maintenance of the sharp band boundary is most important to obtain highly enriched isotope at the boundary region. Light isotope of 14N was enriched at the front boundary and the heavy isotope 15N was enriched at the rear boundary.
The two parameters of separation coefficient and HETP can be calculated from both front and rear boundary regions and the values were listed in Table 2.The observed ε at front and rear boundary should be coincident each other. As shown in Table 2, the observed separation coefficients at front and rear boundary are in good agreement in each Run. The separation coefficient is an equilibrium factor and should be constant, being independent of the migration distance. It is confirmed from the results listed in Table 2 in the cases other than Run1. The small values of separation coefficient of Run1 are probably due to the feed material of (NH4)2SO4 solution and one in NH4SO3-R in the ion exchange resin are resemble each other. In such case, isotope effects do not occur between the two chemical species. Due to this fact, the effective length of migration is reduced by approximately 20%. This effect is reflected in the decrease in the separation coefficient in Run1.
It is also confirmed that the values of ε obtained from Run 4 are slightly reduced. Probably this is due to the remixing in the middle of the adsorption band. Figure 5 showed the chromatographic profile of Run 4. From the figure it can be seen that the isotopic plateau region is not seen, the enriched zone and the depleted zone are directly contacted because of the long migration. It should be noted that the values of ε obtained from the experiments using natural nitrogen (Run 3) are practically the same as those observed by using enriched nitrogen (Run 5);
|Run||Max. enrichment(%)||βrear = rmax/ro||Separation coefficient HETP (mm)|
|Front 14N Rear 15N||Front Rear Front Rear|
|Run 5 used 80% 15N as feed solution, of which ro =4.|
The maximum enrichment β values are defined as the local enrichment factor of 15N at the boundary as follows:
Where r is the isotopic abundance ratio of 15N against 14N. The values of β calculated are listed in Table 2 and plotted as a function of migration distance in Figure 6. The slope of plots is unity, which means that the maximum enrichment β values are proportional to the migration distance up to 30 m. This fact suggests that the enrichment proceeds, forming an ideal shape of exponential enrichment curve at the band boundary region. In addition, it is quite interesting that β value of Run 4 using natural nitrogen is in very good agreement with that of Run 5 where 80% enriched nitrogen was used as feed material. This information is important and useful for designing the enrichment plant based on the present method of ion exchange chromatography.
In order to evaluate the efficiency of nitrogen enrichment in chromatographic migration, HETP is introduced and the calculated values of HETP are listed in Table 2. HETP values are small enough in the rear band region of Runs 1-4 where the enrichment of 15N is steadily proceeding. Similar phenomenon is observed in the front 14N enrichment zone of Run 5. In general, the HETP values are small when the enrichment process does not reach the high level. On the other hand, saturation of isotope enrichment gradually takes place and slope of the enrichment curve sharply decreases when high enrichment is attained. This is the case for the enrichment of 14N in Runs 1-4 and the enrichment of 15N in Run 5.
The results of Run 1-4 clearly indicate that the practical limit of 14N enrichment by the ion exchange packed column is 99.99%. The reason for this limit has not yet been elucidated, but it is estimated that this limit of 99.99% may be applicable for the enrichment of 15N as well. So far, the target of 15N enrichment for nitride fuels is 99.9%. The present work realized the enrichment of 99.678% 15N in Run 5. The results suggest that the 99.9% 15N is attainable by ion exchange enrichment.
6. The effect of cross linking to the nitrogen isotope separation
Separation and concentration of a stable isotope from an isotopic mixture with natural occurrence is a very complex problem and usually, the isotopic separation coefficients of natural abundance are very low. In general, cation exchange process is a promising technique to produce highly enriched isotope due to the nature of small HETP value. Among the operating parameters in cation exchange process, cross linking is known as a decisive factor on the process of nitrogen isotope separation. It is interesting to evaluation the chromatographic performance of 15N isotope separation by ion exchange resin with different percentage of cross linking.
The cation exchange resins with different cross linking were synthesized from the law material of styrene and the synthetic method was given in Figure 7. When different cross
linking was synthesized, high cross linking means high divynybenzene (DVB) materials contained in the resin structure and this means the percentage of ion exchange functional group was decreased in the same amount resin. The relationship between 15N enrichment percentage and cross linking with 2.0 m migration was given in Figure 8. Enriched 15N isotopes were decreased from 0.93 to 0.68 when compared with the cross linking of twenty and forty percentage. Since high cross linking means low exchange capacity, it is reasonable that the 15N enrichment percentage is reduced with the increase of cross linking at the same given migration distances. SQS-6 resin has 8% cross linking and 15N enrichment percentage was 1.56% when SQS-6 resin was performed under the same condition, and low cross linking resin has much higher enrichment ability than high cross linking resin.
The observed HETP values of different cross linking were plotted in Figure 9. It is seen in the figure that cross linking can affect the HETP value obviously. HETP value proportionally increase with the cross linking at the present work and low cross linking has much advantage for HETP. HETP value of 0.036 cm was obtained at the present system by using 20% cross linking and the present resin can be used for the large scale of nitrogen isotope industrial production.
7. Preparation of highly enriched 15N by chemical exchange
The migration distance and cross linking can both affect the nitrogen isotope separation. It has relatively low separation coefficient by ion exchange chromatographic method when compared with that of NITROX method, it is very difficult to prepare 99.9% 15N directly from natural abundance of 0.366%. At the present stage of industrial factory, NITROX was used widely to produce various percentages of 15N products. It is very difficult to get highly enriched 15N by this method. In order to improve feasibility of this method, one good idea is to combine NITROX method and ion exchange chromatography. Starting from the natural abundance, NITROX has advantage to enrich 15N because of large separation coefficient; while when it reaches to relative highly enriched 15N, due to the good merit of very small HETP value, the ion exchange chromatographic method is performed to get highly enriched 15N.
In order to simulate the industry scale, large diameter column (ϕ=3.0 cm) and high speed band velocity were used in this stage. 100 g commercial NH4Cl (15N-80%) were feed into 3.0 cm diameter ion exchange columns. In order to shorten the ammonium adsorption time, the concentration of NH4Cl was adjusted to about 0.5 mol/dm3 and the length of ammonium adsorption band was 138 cm. Then 0.22 mol/dm3 NaOH was feed to the rear part of ammonium adsorption band to develop the adsorption band. The flow rate of feeding solution is 50 ml/min and the band velocity is 12 m/d. When the front boundary of ammonium adsorption band reached to twenty five meters, the three way valve was connected to the column for portion sampling. The sampling volume for each sample was about 0.5 ml for every seven minute and it’s corresponding to 5.0 cm of adsorption band for each sampling. These samples were analyzed by mass spectrometer for determine the nitrogen isotopic ratio as the result of the migration distance equal to 25 meters. When the rear boundary of ammonium adsorption band passes through the three way valve, the sampling was stopped. In order to keep the length of ammonium adsorption band constant and to avoid band diffusion, total amount of 3.0 L pure water with same flow rate was feed to the top of the column to develop the inside part of free ammonium molecular of adsorption band, the free ammonium molecular was move to the front boundary and re-adsorb again at the front boundary. The adsorption band moved forward 22.5 cm after 3.0 L pure water washing. Five days later, NaOH solution was feed again to develop the migration distance until fifty meters. The operation condition was the same with the first stage. When the front boundary of ammonium adsorption band was reached to fifty meters, three way valve was connected to the column for portion sampling. The sampling volume for each sample was about 0.5 ml for every five minute and it’s corresponding to 4.0 cm of adsorption band for each sampling. Before the rear boundary of ammonium adsorption band reach to three way valve, about 10 cm left the boundary, sampling was changed to whole fraction sampling and the volume of each sampling was 30 ml and each corresponds to 1.0 cm of adsorption band, the sampling time was 45 second. Before sampling, excess amount of HCl was added to each bottle for neutralization. After the rear boundary pass through three way valve, 3.0 L pure water was feed to the top of column.
The large scale experimental conditions and results were listed in Table 3 and the chromatographic isotopic distribution curve of 25 m and 50 m migration distance were given in Figure 10 and Figure 11. During the long chromatographic operation, small amount ammonium ion exists in the tailing and may cause to the decrease the final isotope separation effect; this is the disadvantage of the long chromatographic operation. From the isotopic ratio curve of Figure 10 and Figure 11, the front boundary of ammonium adsorption band, the 14N isotopes could be continually enriched to over 99% which starting from 20%. On the contrary, 15N isotope was enriched in the rear boundary regions steadily. Compare the results by Run1 and Run2 in Table 3, both are starting from 80%-15N NH4Cl, the main differences are column diameter and flow rate. In Run3, high flow rate (50 ml/min) and 3.0 cm diameter column was used. The results show that at the rear band, both results have nearly the same values of separation coefficient (0.022) and HETP (0.16cm). At Run3, the highest percentage of enriched 15N was 99.756%, higher than the value of 99.672% by Run2, even if the migration distance in Run3 is shorten than Run2. This means the speed of ion exchange between sodium and ammonium is very fast, and high flow rate does not affect to the HETP and separation coefficient in this operation systems. It is obviously that high flow rate has advantage to get highly enriched 15N and is much suitable to industrial operation. Run 3 and Run 4 were within the same experiment in a whole experiment; here it was divided into two parts. From the results of Run3 and Run4, 15N was steadily enriched with
|Run No.||Run 1||Run 2||Run 3|
|Resin||SQS-6 high porous cation exchange resin|
|Feed solution||0.19M NH4Cl (15N-80%)||0.50M NH4Cl (15N-80%)||0.50M NH4Cl (15N-80%)|
|Effluent solution||0.20M NaOH||0.23M NaOH||0.24M NaOH|
|Migration distance m||30||25||50|
|Column diameter mm||8||30||30|
|Ammonium adsorption band m||1.0||1.38||1.38|
|Flow rate ml/min||1.5||50||50|
|Band velocity m/d||4.8||11.1||14.4|
|Adsorption capacity Q mmol/m||74.3||1230||1250|
|Slope coefficient Ks||0.6104||0.1541||0.5218||0.1569||0.4919||0.1599|
the increase of the long migration distance, but the increasing trend becomes very low. For the first twenty five meter’s migration, 15N has been enriched to 99.756%, after another twenty five meter’s operation, the final maximum enrichment percentage reached to 99.859%. Enriched 15N is only increased 0.1% by another twenty five meter’s migration, although the highly enriched regions became broaden and we can get much volume of 15N which the percentage is over 99.8%. The separation coefficient of Run3 and Run4 is same because of the same operation condition; Run4 has relatively smaller HETP value than the value of Run 3. It indicates that long chromatographic operation has advantage and can steadily enrich 15N to very high percentage. The reason why the enriched 15N could not enrich to higher percentage in the present operation system may come from the stopping during the operation between Run3 and Run4. Because of the stopping by one week, the inner ammonium adsorption band may take remixing within the middle adsorption band. Highly enriched 15N at rear band will mix with middle level enriched 15N which was located in the middle band. If this operation restarts again, it will take long distance chromatographic operation to compensate the mixing and reach to the same percentage of 15N with twenty five meter’s operation. From this result, the effective migration distance may be less than fifty meters. This can be confirmed by the analysis of the isotopic curve of Run 3 and Run 4 in Figure 10 and Figure 11. In Figure 10, there is a flat regions existing in the middle ammonium adsorption band, in this region, the ratio of 15N/14N is the same with
the original feeding solution, 80%. At the rear boundary of the isotopic distribution curve, the slope of isotopic curve is still kept sharpness. In Figure 11, it was found that this flat region almost disappears and the isotopic ratio of 15N/14N was steadily increasing in the whole ammonium adsorption band. At the rear boundary region of the isotopic curve, there is a large amount of highly enriched 15N and the slope coefficient of isotopic distribution curve becomes flat. This is the evidence that by long chromatographic operation, highly enriched 15N was remixing again with the middle level enriched 15N in the middle position of ammonium adsorption band. The percentage and gram distribution of enriched 15N which along with ammonium adsorption band were listed in Table 4. 15N was mainly concentrated in the adsorption band which range from 64.5-152.03 cm in the adsorption band and 4.6 gram of highly enriched 15N(>99.82%) were successfully obtained.
|Adsorption band length|
|Percentage distribution of 15N|
|28.5～ 33||4.118 ～ 35.32||0.3539|
|33 ～ 46.5||35.32 ～ 80.39||2.2598|
|46.5 ～ 64.5||80.39 ～91.81||3.2737|
|64.5 ～ 82.5||91.81 ～ 98.73||3.5679|
|82.5～ 123||98.73～ 99.79||8.1944|
|123 ～147.3||99.79 ～99.86||4.6148|
|147.3～ 152.03||99.86 ～ 99.69||0.8185|
8. Conclusion of nitrogen isotope separation by ion exchange method and the comparison with NITROX separation method
Long chromatographic operations were studied to nitrogen isotope separation by using 80% enriched 15N-NH4Cl. The main purpose was to get very highly enriched 15N isotope and to study how the flow rate and column diameter affect to nitrogen isotope separation. From the results obtained by each runs, it was confirmed that front and rear boundary could enrich 14N and 15N steadily to very high percentage. Since the feeding and elution solution are same for Run 1, Run 2 and Run 3, the same separation coefficients should be obtained no matter the migration distance. Due to the small amount of ammonium remained on the column, separation effect became slightly decrease with long chromatographic migration distance, especially by large diameter columns. When compared with the results of Run 2 and Run 3, the HETP value of Run 3 is smaller than Run2.
During the long operation, 15N can be steadily enriched to very high purity. Because the remixing phenomena take place, the highly enriched 15N will penetrated into the middle band, it decreased the maximum enrichment percentage of 15N, but the highly enriched zones became broadened with long migration distance. The maximum percentage of enriched 15N was 99.859% and 4.6 gram of highly enriched 15N (99.82%) were successfully obtained by fifty meter’s operation.
Chemical exchange of nitrogen oxide system has been discussed for nitrogen isotope separation deeply in early times. Fifty years ago, W.Spindel and T. Taylor performed nitrogen isotope separation by chemical exchange (NITROX) with the condition of 15 ml/min of 10 mol/dm3 nitric acid, containing the natural 15N abundance . They produced material containing 6.0 g of nitrogen analyzing 99% 15N by twenty-five days continuously columns operation. Because of the large separation factor (1.055) by using NITROX method, most of industrial scale plants in the world are adopted with this method to produce nitrogen isotopes. As mentioned above, ion exchange method has the advantage of very small HETP, it can obtain very highly enriched nitrogen isotopes and no large amount of waste gas and liquid occurred, it can be widely used if combined with NITROX method when 15N has been enriched to the percentage of, for example, 80%. One problem come from ion exchange method is the capacity of resin. The ion exchange NH4-R/NH3aq on cation exchange resin being inefficient for large scale production, according to the small flow rate accepted in the separation columns. That involves utilization of too large diameter separation columns with prohibitive amount of cation exchange resin.
Taking into account that the world market is about 20 to 40 Kg 15N annually, the supply of that isotope for nitride fuel production for nuclear power reactors (NPR) and accelerator driven system (ADS) would therefore demand an increase in production capacity by a factor of 1000. For an industrial plant producing 100 t/y 15N, using present technology of isotopic exchange in NITROX system, the first separation stage of the cascade would be feed with 10M HNO3 solution of 600 ml/h flow rate. If conversion of HNO3 into NO, NO2, at the enriching end of the columns, would be done with gaseous SO2, for a production plant of 100 t/y 15N, a consumption of 4 million ton SO2/y and a production of 70% H2SO4 waste solution of 4.5 million ml/y are estimated. The reconversion of H2SO4 into SO2 in order to recycle of SO2 is a problem to be solved to compensate the cost of SO2, and to diminish the amount of H2SO4 waste solution. If it’s considered that all ADS installations for minor actinides transmutation utilize nitride fuel with 15N, the need of that isotope is about 4 t/y, with a cost of 400 million USD (the price of 15N was considered 100 USD). It should be taken into consideration an important price reduction of 15N in order to make possible its utilization for large scale production of nitride fuel for NPRs and ADSs.
The authors would like to express best thanks to Professor Yasuhiko Fujii, Dr. Tatsuya Suzuki and Dr. Masao Nomura, Research Laboratory for Nuclear Reactors, Tokyo Institute of Technology, Japan for their kindly guidance in technical and material supporting.