SEPARATION OF CARBON-13 BY THERMAL

DIFFUSION

GHEORGHE VASARUAleea Tarnita, Nr. 7, Apt. 11

400649 CLUJ-NAPOCA, ROMANIAE-mail: gvasaru@hotmail.com

ABSTRACT

In the selection of a process gas for use in the separation of 13C by thermal diffusion, methane is a first candidate because of its low molecular weight. Generally, the process equipment to be employed for this separation consists of concentric tube columns with calrod heaters, which are normally operated at a mean temperature no more than 673 K because methane decomposes at greater temperatures.

This paper gives a short overview of the most important applications of 13C and describes a thermal diffusion cascade for enrichment of this isotope.

Successively, the results of calculations of the transport coefficients H and K for a concentric tube column, operated with methane as process gas, are presented. Static separation factor at equilibrium vs gas pressure has been calculated for various molecular models. The experimental separation factors for different gas pressures were found to be consistent with those calculated for the inverse power repulsion model and the Lennard-Jones (12,6) model.

Thermal Diffusion Process

The thermal diffusion process is based on the fact that molecular diffusion can be caused by a temperature gradient. In general, i f two gases are exposed to a temperature gradient between two surfaces, the gas with the lower molecular weight wil l tend toward the hotter surface. The two gases wil l separate unti l a concentration gradient occurs result ing in concentration diffusion of equal magnitude in the opposite direction. Under equil ibrium condit ions the rate of transfer of the l ight molecules towards the hot surface resulting from thermal diffusion wil l be exactly counterbalanced by concentration diffusion.

In a thermal diffusion column the relatively small separation factor is multipl ied by the effect of convection currents result ing from the temperature gradient. The heavy molecules, which tend toward the cold surface, are swept to the bottom of the column while the l ight molecules at the hot surface are swept toward the top of the column. The maximum separation is l imited by the concentration diffusion that is eventually set up in the axial direction as a result of the separation i tself.

Thermal Diffusion Process (Cont’d)

This transport phenomena makes available enriched isotopes which either cannot be provided by other separation methods or are more costly when prepared by alternate means with emphasis on concentrating isotopes of the inert gases. The heaviest and l ightest isotopes in such mixtures can easily be enriched to any desired concentration if a proper thermal diffusion cascade is constructed [1- 4]. A cascade to enrich an isotope of other than the greatest or least mass in a mixture of three or more components become more complicated in arrangement and offers design problems relative to length, width and f low rates.

Construction of thermal diffusion column presents engineering problems associated with supported heated central elements. At the present t ime, thermal diffusion columns are designed to use standard, commercial tubular heaters or wire heaters with an effective length of some meters. To conserve space, 12 to 19 columns are enclosed in a common water jacket. Thus, individual columns can be interconnected externally to give any desired shape of cascade. Within the same bundle, some columns can be used for enriching one isotope, while at the same time other columns are being used to enrich a different isotope.

The Transport Equation

The transport equation for a thermal diffusion column is:

(1)

where τ is the total transport of required isotope, H is the coefficient of transport by thermal diffusion, c is the fractional molar concentration of the required isotope, Kc is the coefficient of transport by convection currents, Kd is the coefficient of transport by ordinary diffusion, and z is the axial coordinate of the column. Kc and Kd are named also as convective and diffusive remixing coefficients, respectively. According to the Jones and Furry theory [5], H and Kd are functions of pressure; thus

(2)

Kd is independent of pressure.

The Transport Coeff icients for Cylindrical Case

The transport coefficients for the cylindrical case of a TD column and for the Lennard-Jones (12-6) molecular model are given by the following expressions:

(3)

(4)

(5)

where αT is the TD constant, ρ - the density, η -- the viscosity, D - coefficient of ordinary diffusion, all at the temperature of the cold wall, T1, g - the gravity constant, r1 - the radius of cold

wall, h, kd and kc - shape factors, θ = T2/T1, R = r1/r2, -

the reduced cold wall temperature, T2 and r2 - temperature and radius of hot wall, respectively, k - Boltzman constant and ε - the depth of potential well.

Equil ibrium Separation Factor

Putting in (1), τ = 0, we have

(6)

the integral of which is

(7)

or equivalently

(8)

If z0 ≤ z ≤ L and c0 ≤ c ≤ cL, where L is the length of the thermal diffusion column, we have for the equilibrium separation factor the expression

(9)

The Separation Factor per Mass Unit

The separation factor per mass unit, Q*, is given by the equation:

(10)

where H* = coefficient of thermal diffusion transport per unit mass, Kc = coefficient of convective remixing, Kd = coefficient of diffusive remixing, Kp = coefficient of parasitic convection L = length of column The coefficient of parasitic remixing, Kp, arises due to unknown inaccuracies within the column such as nonuniform surface temperature distribution and imperfect centering of the heater.

Transport Coeff icients vs PressureThe H*, Kc and Kd factors can be written as function of pressure and take the form

(11)

where a, b, and c are constants determined by column geometry and temperature and by properties of the gas. The ratio b/a and c/a can be determined from the equilibrium data, but a different kind of experiment must be performed to estimate a and allow calculation of b and c. These ratios may be computed from the equations [6]:

(12)

where p = gas pressure at which the maximum separation factor occurs, Q* = separation factor per unit mass at the maximum in the curve. Pressure at the maximum separation.

When the gas pressure in a thermal diffusion column is adjusted to achieve maximum separation, the coefficient of convective remixing, Kc, is equal to the coefficient of diffusive remixing, Kd,

Heat Losses

Heat is removed in four ways from the heating element in a thermal diffusion column: by radiation from the heater, by convection currents in the gas, by conduction through the gas, and by conduction through the spacers between the heater and the cold wall and lengthwise through the heater sheets to the cold jacket end f itt ings [7].

Convection and conduction through the gas are essential for the operation of a thermal diffusion column, but i f the heat loss via radiation or direct conduction through the spacers can be decreased, the over-al l economy of operation wil l increase. Theoretical and experimental investigations of heater temperature and various modes of heat transfer to the cold wall were undertaken to better understand column operation and to increase the efficiency and economy of isotope separation by thermal diffusion.

The amount of heat radiated from the heater and the amount conducted through the spacers and sheets can be determined from power input and heater sheath temperature with an evacuated column .

Tapered Cascade

I f an eff icient tapered cascade is to be designed to enrich an isotope from some small concentration to some higher concentrations, the thermal diffusion characteristics of a given column system must be determined. These characterist ics can be computed theoretically. To test the validi ty of this theory, a series of experiments was performed to determine the agreement between observed values of thermal diffusion separation factors and the theoretical values calculated according to Jones and Furry theory.

The theoretical and observed separation factors for 13CH 4, as function of gas pressure show that the maximum equil ibrium separation factor occurs at a lower pressure.

Comparison of Separation Methods

Research needs for 1 3C include nuclear bombardment studies, tracer studies on chemical react ion and biological processes and cl inical medicine studies.

Most molecules of biological interest are large and complex. Synthesis with 1 3C requires several react ions each having a relat ively low yield. Consequently, the several grams of 1 3C would be required to synthesize 1 g of a carbon biological molecule. Thus, i f 1 3C is to be a practical tool in biological research, i t must be available in larger quantit ies at a lower cost.

For producing large quantit ies of enriched carbon-13 from natural abundance carbon (1.1 % 1 3C and 98.9 % 1 2C), R.A.Schwind [8] performed an economic evaluation of four methods: thermal dif fusion, dist i l lat ion, gaseous dif fusion and chemical exchange. These processes were chosen because they are only ones for which enough laboratory and production knowledge is available to design large product ion facil i t ies. From this study, the relative production cost per gram of 1 3C of a mixture containing 60 % 1 3C was obtained as a funct ion of the production rate for each of these methods. The cost f igures were based on an amort ization of the capital equipment cost over a period of 10 years.

Practical Conclusions

The practical conclusions are as follows: Thermal diffusion was found to be most economical method for the production rates below 100 g/a; CO disti l lat ion should be used for production rates above 200 g/a. The gaseous diffusion and the CO

The world’s largest unit for 13C production is located in Xenia, Ohio, at Cambridge Isotope Laboratories Inc [9] This plant has been in continuous operation since 1990 producing 99 % 13C at a rate of 30 kg/a. After the current expansion in 1997, the plant capacity has been increased to 120 kg/a. The recent increased interest in this unique isotopic material fol lows regulatory approval of the f irst diagnostic test which uses 13C. Recently, the FDA gave approval for cl inical use of the 13C Urea Breath Test for the detection of the ulcer-causing bacterium Helicobacter pylori. This new breath test is safer, simpler, and more accurate than other tests which diagnose Helicobacter pylori infection. In this breath test, the patient drinks a solution of non-radioactive 13C Urea and then breathes into a collection device. The test takes only thirty minutes; can be performed in a doctor’s off ice; avoids the need for stomach endoscope with biopsy an is more accurate than blood tests.

Separation of 13C by Thermal Diffusion Practical Aspects (I)

A thermal dif fusion cascade has the advantage of being relat ively easy to operate. However, thermal dif fusion is an irreversible process and therefore require a large quantity of energy per gram of material separated. There is also the disadvantage that the basic thermal dif fusion column cannot be scaled up. The gap between the hot and cold walls cannot be increased because the separation factor is proport ional to the temperature gradient and there is a practical l imit to the obtainable temperature difference. The diameter of thermal dif fusion columns cannot be increased above a certain l imit because temperature in homogeneit ies in the hot and cold walls cannot be avoided. For these reasons even a very large-scale thermal dif fusion plant must be composed of relat ively small diameter thermal columns. A simplif ied scheme of our standard thermal dif fusion column are given in Fig. 1.

The standard thermal diffusion column of concentric tube type:

1,15 – electrical contact rods; 2,14 – connecting tubes (brass); 3,4 – textolyte insulators; 5 – flange (stainless steel); 6,10 – rubber gaskets; 7 – cold wall; 8 – hot wall; 9 – spacer; 11 – lower end of the hot wall; 12 – bellows; 13 - flange (copper).

Separation of 13C by Thermal Diffusion Practical Aspects (II) At low production rates, the cost of labor is the controll ing factor and the thermal dif fusion

is an attractive process. One of the most persistent problems encountered in the 1 3C thermal diffusion

cascade is decomposition of the process gas (methane) into free hydrogen and carbon. Since this decomposition could be catalyzed by the surface of central heater, a series of experiments was conducted to evaluate methane decomposition on various metal surfaces Using a heater made by swaging a soft aluminum sheath over the standard stainless steel calrod, no perceptible decomposition of methane was observed at 673 K.

The performances of several methane thermal diffusion cascades for 1 3C enrichment from natural abundance was calculated. To guide current laboratory operations, various arrangement of the existing 19-column cascade were evaluated. From the six alternatives we have selected the cascade arrangement of 8-4-2-1-1-1-1-1 columns per stage from feed to product withdrawal, respectively, Fig. 2 [10]. This cascade was set up with an appropriate system for feed purif ication, pressure control, waste and product withdrawal, impurity control and removal, and stages gas circulation. In the feed system, methane of 97.4% purity was further purif ied by pumping volatile impurit ies, at l iquid nitrogen temperature, up to 99.85 - 99.88%. After purif ication, the methane was stored in a high-pressure bottle from which it was fed through a special system into the feed reservoir. Waste, i.e. depleted methane in 1 3C was withdrawn from the feed reservoir and stored as methane of high purity.

Enriched methane in 1 3C was removed continuously from the bottom of the seven stages and stored in a calibrated reservoir.

Separation of 13C by Thermal Diffusion Practical Aspects (III) The methane used as feed gas was not completely free of impurit ies such as nitrogen,

carbon dioxide and ethane. These impurit ies introduced with the feed material in cascade are transported at a high rate towards the bottom of the cascade where they accumulate. If these are not removed continuously, the fairly sharp interface between methane and impurit ies rises rapidly and the effectiveness of the separation system is destroyed [11] . For removing these impurit ies a single column was provided, column 19, placed at the bottom of the cascade. The level of impurit ies was detected with a thermal-conductivity cell placed at the bottom of the column 19. For reference the enriched methane from the bottom of the seven stage was used. The signal of these sensors was a direct measure of the methane purity in the column. Impurit ies were withdrawn from the bottom of column 19 through a calibrated leak.

For interstage gas circulation, hermetically sealed compressors was used. Allowing only one column at a moment, in each stage, to be open to the compressor-driven loop obviated the parasitic gas circulation. The columns in stages 1 - 3 were alternately opened to the circulation manifold by solenoid valves operated by an electronic programmer.

The control of enriching during the transient period has been performed by mass spectrometry.

The cascade was operated at the temperature of 673 K, all 19 thermal diffusion column having a single cooling jacket in a bundle system, maintained at the temperature of 293 K. The operating pressure was of 1.05 at.

Parameters of the Methane Thermal Diffusion Cascade

Physical Properties of Methane (at T 1 = 295 K): Density, ρ (g/cm 3) 6.626x10 -4

Viscosity, η (g/cm.s) 1.110x10 -4

Diffusivity, D (cm 2/s) 0.215 Thermal diffusion constant, α T 0.00678 Carbon Isotopes: 1 2C (98.892%); 1 3C (1.108%) Target: The enrichment of 1 3C at the concentration of 25% 1 3CH 4 Geometric Parameters and Operating Conditions: Radius of cold wall, r 1 (cm) 1.725 Radius of hot wall, r 2 (cm) 0.900 Column length, (cm) 400 Temperature of the cold wall, T 1 (K) 295 Temperature of the hot wire, T 2 (K) 673 Operating pressure, p (at) 1.04 Power consumption per column (kW) 1.7 Materials: hot wall: stainless steel; cold wall: brass Transport Coefficients (LJ model): H (g/s) 4.50x10 -5

K c (g.cm/s) 2.40x10 - 2 K d (g.cm/s) 1.37x10 -3

Q e (exp.) per column 2.00 Cascade: 19 columns of concentric tube type in 8 stages Cascade Configuration (Staging from the waste end): 8-4-2-1-1-1-1-1 Production: 1 3CH 4 at the concentration of 25% 1 3C (g 1 3C/year): 33

Thank you!

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