ANALYTICAL STUDY OF CATALYTIC REACTORS FOR HYDRAZINE ... · Analytical Study of Catalytic Reactors...

NASA UARL H910461-38

THIRD ANNUAL PROGRESS REPORT

ANALYTICAL STUDY OF CATALYTIC REACTORS FOR HYDRAZINE

DECOMPOSITION B

-+ 8 by

Arthur S. Kesten

prepared for

NATIONAL AERONAUTICS AND SPACE ADMINISTRATION

May, 1969

CONTRACT NAS 7-458

United Qircraft Research Laboratories

UNITED AIRCRAFT CORPORATION

-FI E A S T HARTFORD. CONNECTICUT

https://ntrs.nasa.gov/search.jsp?R=19690023881 2020-03-25T14:02:25+00:00Z

NASA UARL H910461-38

THIRD ANNUAL PROGRESS REPORT

ANALYTICAL STUDY OF CATALYTIC REACTORS FOR HYDRAZINE

DECOMPOSITION

by Arthur S. Kesten

prepared for

NATIONAL AERONAUTICS AND SPACE ADMINISTRATION

May, 1969

CONTRACT NAS 7-458

United FIircraft Research Laboratories

U UNITED AIRCRAFT CORPORATION

EAST HARTFORD. CONNECTICUT

Report 11910461- 38

Analytical Study of Catalyt ic Reactors

for Hydrazine Decomposition

Third Annual Progress Report

April 15, 1968 - Apri l 14, 1969

Contract NAS 7-458

TABLE OF CONTENTS

Page

A B S T R A C T , . . . . . . . . . . . . . . . . . . . . . . . . . . . . . i

FOREMORD . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . ii

S M M Y . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1

INTRODUCTION . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2

DESCRIFTION OF THE TRANSIENT MODEL 3

RESULTS OF CALCULATIONS. . . . . . . . . . . . . . . . . . . . . . . 10

REFERENCES.. . . . . . . . . . . . . . . . . . . . . . . . . . . . 14

LIST OF SYMBOLS. . . . . . . . . . . . . . . . . . . . . . . . . . . 15

A P P E N D I X . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 18

FIGURES . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25

. . . . . . . . . . . . . . . . .

ABSTRACT

Analytical s tudies of catalyzed hydrazine decomposition reaction chambers were performed i n order to es tab l i sh procedures capable of predict ing the e f f ec t s of pulse operation of t he reactor fo r an a rb i t r a ry duty cycle on the t rans ien t behavior of the system. These s tudies included an extension o f a computer program previously developed t o calculate temperature and reactant concentrations as functions of time and a x i a l posi t ion i n typ ica l reaction chamber configurations. The extended program includes consideration of t he e f f ec t s of heat conduction and d i f f i s ion when flow i s stopped. I n addition, reaction chamber f l u i d dynamics are taken in to account by allowing fo r feed pressure and mass flow r a t e changes with time. The e f f ec t s of these changes on thermal and ca t a ly t i c decomposition of reactants , along with heat and mass t r ans fe r between the free-gas phase and the gas within the pores of the ca ta lys t p e l l e t s , a r e considered.

A s e r i e s of caluclat ions was made using the computer program t o evaluate the e f f ec t s o f duty cycle, nominal 'chamber pressure, bed loading, and ca ta lys t bed configuration on the t rans ien t temperature, pressure, and reactant con- centrat ion d is t r ibu t ions i n the reactor system. The r e s u l t s of these calcu- l a t ions are i l l u s t r a t e d i n the report .

i

FORENORD

This work was performed by United Aircraf t Research Laboratories f o r the National Aeronautics and Space Administration under Contract NAS 7-458 i n i t i a t e d Apri l 15, 1966.

Included among those who cooperated i n performance of the work under Contract NAS 7-458 were D r . A. S. Kesten, Program Manager, Dr. W. G. Burwell, Chief, Kinetics and Thermal Sciences Section, M r . D. B. Smith, and Mrs. E. Smith of UARL.

This work was conducted under program management of the NASA Chief, Liquid Propulsion Experimental Engineering Systems, NASA Headquarters, Washington, D. C . , and the Technical Manager was M r . T . W. Pr ice , J e t Propulsion Laboratory , Pasadena, Cal i fornia .

ii

Report H910461-38

Analytical Study of Catalyt ic Reactors

f o r Hydrazine Decomposition

Third Annual Progress ReDort

Apri l 15, 1968 - April 14, 1969

Contract No. NAS 7-458

SUMMARY

The Research Laboratories of United Aircraf t Corporation under Contract NAS 7-458 with the National Aeronautics and Space Administration have been performing an ana ly t ica l study of c a t a l y t i c reactors fo r hydrazine decomposi- t ion . This t h i r d annual technical report summarizes work performed under t h i s contract from Apri l 15, 1968 t o April 14, 1969. period has included t h e development of a computer program representing a t rans ien t model of a distributed-feed catalyzed hydrazine decomposition reaction chamber. The model describes the behavior of reactors operated under conditions of continuous flow as well as pulsed flow for an a rb i t r a ry duty cycle. Both thermal and ca t a ly t i c decomposition of reactants a re considered along with simultaneous heat and mass t r ans fe r between the free- gas phase and the gas within the pores of the ca ta lys t p e l l e t s . e f f ec t s of heat conduction and diffusion when flow i s stopped are included i n the model. I n addition, react ion chamber f l u i d dynamics are taken i n t o account i n order t o allow consideration of chamber pressure and mass flow r a t e changes with time. and species concentration d is t r ibu t ions as functions of time and axial posi t ion i n typ ica l hydrazine react ion chambers fo r a number of pulse duty cycles, mass flow r a t e d is t r ibu t ions , and ca ta lys t bed configurations.

Work during t h i s

The

Calculations have been made of temperature

Calculated t rans ien t temperature p ro f i l e s i n a continuous flow reactor

Generally good agree- have been compared with temperatures measured as a function of time i n a small scale engine run at J e t Propulsion Laboratory. ment between theo re t i ca l and experimental r e s u l t s w a s found.

The computer programs representing both the steady-state and t rans ien t models of a catalyzed hydrazine reactor have been described i n d e t a i l i n t w o computer manuals. These manuals contain operating ins t ruc t ions f o r these programs as well as descriptions of input and output formats.

1

H910461-38

INTRODUCTION

Under Contract NAS 7-458, t he Research Laboratories o f United Aircraf t Corporation are performing ana ly t ica l s tudies of the behavior of dis t r ibuted- feed ca t a ly t i c reactors f o r hydrazine decomposition. The spec i f ic objectives o f t h i s program are ( a ) t o develop computer programs f o r predict ing the temperature and concentration d is t r ibu t ions i n monopropellant hydrazine ca t a ly t i c reactors i n which hydrazine can be in jec ted a t a rb i t r a ry locat ions i n the reaction chamber and (b ) t o perform calculations using these computer programs t o demonstrate t he e f f ec t s of various system parameters on the performance of t h e reactor .

Progress previously reported i n the f irst annual report (Ref. 1) included the development of computer programs which describe the steady-state and t rans ien t behavior of a hydrazine reactor operated under conditions of constant, continuous flow, i n which complete radial mixing i n the free-gas (or l i qu id ) phase $as assumed. Progress previously reported i n the second annual report (Ref. 2) i n c l u e d an extension of the steady-state program t o include r a d i a l as well as axial var ia t ions i n temperature and concentrations i n order t o permit an analysis of various in jec t ion schemes and ca t a lys t bed configurations which exhibi t r a d i a l nonuniformities. been used t o calculate temperature and reactant concentration d is t r ibu t ions as functions of i n i t i a l bed temperature, feed temperature, chamber pressure, mass flow r a t e d is t r ibu t ion , ca t a lys t s i ze d is t r ibu t ion , and ax ia l i n j ec to r locations.

These programs had

During the t h i r d year of contract e f f o r t a t ten t ion has been focused on extending the t rans ien t model of t h e reactor system t o take the e f f ec t s of react ion chamber f l u i d dynamics on t rans ien t response in to account, and t o permit consideration of pulse operation of the reactor fo r an a rb i t r a ry duty cycle. I n addition, computer manuals have been prepared describing t o poten t ia l users t he operation of both the steady-state and-transient computer programs (Refs. 3 and 4 ) . Included i n suceeding sections of t h i s report are de ta i led descriptions of (a) the development of t he equations representing the t rans ien t model of t he reactor system, ( b ) the use of t h e computer program representing the t rans ien t model t o compute t rans ien t temperature pro- f i l e s i n a typ ica l continuous flow reactor i n order t o t e s t the v a l i d i t y o f the model by comparing the calculated r e s u l t s with measured temperature p ro f i l e s , and ( c ) t he use of the t rans ien t computer program t o calculate the e f f ec t s on t rans ien t temperature and reactant concentration d is t r ibu t ions of i n i t i a l bed temperature, chamber pressure, mass flow r a t e d is t r ibu t ion , ca ta lys t s i ze d is t r ibu t ion , and pulse duty cycle.

2

DESCRIPTION OF THE TRANSIENT MODEL

The analysis o f a hydrazine engine reaction system per ta ins t o a reaction chamber packed with ca ta lys t p a r t i c l e s i n t o which l i qu id hydrazine i s in jec ted a t a r b i t r a r i l y selected axial locat ions. Catalyst p a r t i c l e s a re represented as "equivalent" spheres with a diameter taken as a function of the p a r t i c l e s i z e and shape. Both thermal and ca t a ly t i c vapor phase decomposition of hydrazine and ammonia a re considered i n developing equations describing the concentration d is t r ibu t ions of these reactants . Diffusion o f reactants from the free-gas phase t o the outside surface of t h e ca t a lys t p e l l e t s i s taken i n t o account. Since the ca ta lys t mater ia l i s impregnated on the in tep ior and ex ter ior surfaces of porous pa r t i c l e s , the diffusion o f reactants i n to the porous s t ruc ture must a l so be considered. I n addition, t he conduction of heat within the porous p a r t i c l e s must be taken i n t o account since the decomposition reactions are accompanied by the evolution o r absorption of heat .

In generalizing t h e t r ans i en t model described i n Ref. 1 t o consider reac- t o r shutdown as well as s tar t -up, the temperature and the concentration of reactants i n the i n t e r s t i t i a l (free-gas) phase are s t i l l assumed t o vary only with time and a x i a l distance along the bed. I n t h i s system film coef f ic ien ts are used t o describe heat and mass t r ans fe r between the i n t e r s t i t i a l phase and the outside surface of t he ca ta lys t p e l l e t s . cp, and the temperature, Tp, a re taken as uniform within the. i n t e r i o r o f the porous pa r t i c l e s . Heat and mass diffusion within the p a r t i c l e s are taken in to account by multiplying the react ion r a t e s computed on the basis of uniform cp and Tp by a u- t i l izat ion fac tor determined by analogy with the steady-state system (see Ref. 1). reactor operation l i q u i d ve loc i t i e s are su f f i c i en t ly low re l a t ive t o other r a t e processes so tha t , f o r a l l p rac t i ca l purposes, steady-state i n the l i qu id and liquid-vapor regions i s achieved as soon as the l i q u i d reaches a given ax ia l locat ion i n the reactor . No consideration i s given t o regression o f t h e liquid-vapor in te r face as the chamber pressure bui lds up since the overa l l length of t he l i q u i d region i n typ ica l reactors i s very s m a l l compared t o the length of t he vapor region (Ref. 1). When flow i n t o the reac- t o r i s stopped it i s eas i ly shown t h a t the residual l i q u i d hydrazine i n the reactor vaporizes i n j u s t a few milliseconds due t o the very rapid decomposi- t i on of hydrazine i n the l i q u i d region. shutdown, the l i qu id regions plays a very s m a l l r o l e i n determing the t rans ien t behavior of the reactor system.

The reactant concentrations,

I n addition, it i s assumed t h a t during

Therefore, even during reactor

The t rans ien t model i s concerned then with the vapor region only, The general equations describing the, r a t e s of change of enthalpy and reactant concentrations with time and a x i a l distance i n the i n t e r s t i t i a l phase a re

3

11910461- 38

a 6 -$ [Pi h i ] = - dz [Ghi] - HNZH4 rho;6 + F h F

where

Equations (1) through (5) can be reduced to a somewhat simpler form with the aid of an overall equation of continuity which can be written as

4

H g l O & l - 38

Equations (1) through ( 5 ) can now be wri t ten as

The las t term on the r igh t s ide of Eq. (8) represents the heat loss from the bulk vapor t o the w a l l of the reactor. Taking the reactor walltempera- t u r e as uniform, the r a t e of change of w a l l temperature with time i s

adding a

The posi t ion from Eq. terms of

where the l a s t term on the r igh t s ide of Eq. (13) represents t he heat l o s s by forced convection from the reactor t o the surrounding atmosphere. Heat l o s s by na tura l convection o r radiat ion can be represented i n Eq. (13) by

term of t he form AatG (Tw -T )1'25 or AalIAw (T: - T 4 ) , respectively. a a

mass flow r a t e , G, may be calculated as a function of time and axial from the i n l e t mass flow ra t e , which i s a function of pressure, and ( 7 ) . The i n l e t mass flow r a t e a t any time may be calculated i n the steady-state (SS) i n l e t m a s s flow r a t e using

5

H910461- 38

For choked nozzle and for a r a t e of change of vapor density w i t h time which i s approximately uniform throughout t h e reactor , Eq. (7 ) reduces t o

Taking t h e chamber pressure t o be uniform throughout the reactor , the corresponding r a t e of change of chamber pressure with time can be approximated by

A t a given axial locat ion the r a t e s of change of temperature and reactant concentrations i n the ca ta lys t p a r t i c l e s with time are given by

- dc;ZH4 _ - - I N2H4 + 3 - kCN2 H4 ( ~ ~ ~ 2 ~ 4 - dt Q~ ‘het Q P a

6

Q P Q

3MH2 + rh;;3 - 2~ NH3 dt Q P

where the f i l m coef f ic ien ts , .hc , .Aw, and kc, may be estimated from (Ref. 5 )

K i = 4 , = 0.74 GG) + - a

PP

and

It should be noted t h a t t he thermal conduction term i n Eq. (22) and the simple diffusion term i n Eq. (23) become s igni f icant only when the mass flow r a t e i s qui te s m a l l , as it i s during reactor shutdown.

Recalling t h a t the reaction o f hydrazine on the ca ta lys t surfaces i s extremely fast , so t h a t t he reaction r a t e i s controlled by the r a t e of t ransport o f hydrazine t o t h e ca ta lys t surfaces, Eq. (18) can be used t o define rhetN2H4 by noting t h a t (d%N2H4/dt) and %N2H4 are both approximately equal t o zero. The reaction r a t e is then given by

- 3k:2H4 N2H4 C i

N2H4

'het a

The react ion r a t e of ammonia on the catalyst, surfaces, rhetNH3, can be computed by multiplying t h e r a t e of reaction calculated on the bas i s of uniform T C by the u t i l i z a t i o n fac tor determined by analogy with the steady-state system (see Refs. 1, 6 and 7 ) .

and P

P

7

H910461- 38

This general system of equations i s applicable t o both normal reactor operation and reactor shutdown. s implif ied considerably by noting f i r s t tha t , during the "on" portion of a pulse duty cycle ( o r during continuous reactor operation), gas ve loc i t ies a re so grea t t h a t the time l a g from the entrance t o the vapor region t o any axial pos i t ion f o r t he f l u i d i s negl igible compared with other t rans ien t e f f ec t s . Here Eqs. (8) through (12) may be approximated by

P a r t i a l d i f f e r e n t i a l equations may be

Some simplif icat ion of the p a r t i a l d i f f e r e n t i a l equations may be achieved i n describing reactor operation during the "of f" port ion of a duty cycle by noting t h a t , here, gas v e l o c i t i e s a re su f f i c i en t ly l o w so t h a t t he terms i n Eqs. (8) through (12) involving G a may be approximated when in tegra t ing these equations over s m a l l time in t e rva l s without introducing any s ignif icant e r ro r i n to the calculat ions.

z

8

Fin i t e difference methods have been used t o program f o r d i g i t a l computa- t i o n the d i f f e r e n t i a l equations describing the changes i n temperature and concentrations i n the reactor system. These methods a r e similar t o those discussed i n Ref. 1, where each of t he d i f f e r e n t i a l equations i s t r ea t ed a s an ordinary d i f f e r e n t i a l equation (by in tegra t ing with respect t o time a t a f ixed posi t ion or vice versa) . Each equation i s rearranged i n the form

where the quant i t ies a and p are taken as constant while in tegra t ing the equations from Sk-1 t o Sk (corresponding t o A t or A z ) . integrated t o obtain

Equation (30) can be

where gk i s the value of g at Sky and gk-1 i s the value of g a t Sk-l. a l t e rna t ive form of Eq. (31) i s

An

It i s convenient t o use equations of t h e form of Eq. (31) t o compute p a r t i c l e concentrations and temperatures, and t o use equations of t he form of Eq. ( 3 2 ) t o compute i n t e r s t i t i a l concentrations and temperatures.

The equations representing the t rans ien t model of a hydrazine ca t a ly t i c reactor have been programmed using F9RTRAN I V source language for t he UNIVAC 1108 d i g i t a l computer. i n a computer manual (Ref. 4). and a descr ipt ion of possible operational problems associated with the program.

This computer program i s discussed i n d e t a i l The manual includes input and output descriptions

9

H910461-38

RESULTS OF CALCULATIONS

A se r i e s of calculat ions of t he t rans ien t behavior o f a ty-pical continuous flow reactor fo r which experimental information i s available (Ref. 8) was made i n order t o examine the effectiveness of the t r ans i en t model. The calculat ions per ta in t o a 50 l b f nominal t h rus t hydrazine reactor 2.4 i n . i n diameter i n t o which l i q u i d hydrazine i s in jec ted at the upstream end of the reactor only. The ca ta lys t bed packing was taken t o consis t of 25-30 mesh ca ta lys t p a r t i c l e s f o r the f i rs t 0.25 in . and 1/8 i n . x 1/8 i n . cy l indr ica l p e l l e t s f o r the remainder of the bed. This configuration i s re fer red t o i n the f igures as "mixed bed #l". steady-state mass flow r a t e as 6.5 lb/f t2-sec, and the i n i t i a l chamber pressure as 14.7 ps ia . 4. posi t ions i n Fig. l* fo r a case i n which t h e i n i t i a l bed temperature was taken as 530 deg R. Measured gas temperature p ro f i l e s (Ref. 8) a r e a lso shown i n Fig. 1 f o r purposes of comparison. and experimental r e s u l t s may be noted, pa r t i cu la r ly during the ear ly stages of the t rans ien t . While the differences between measured and calculated r a t e s of response are i n p a r t due t o the thermocouple response time, the use of steady-state u t i l i z a t i o n fac tors t o describe heat and mass diffusion within ca t a lys t p a r t i c l e s under t rans ien t conditions r e s u l t s i n calculated response r a t e s which are a l i t t l e too high. The calculated mole-fraction p ro f i l e s for hydrazine and amnonia, corresponding t o the temperature p ro f i l e s shown i n Fig. 1, are i l l u s t r a t e d i n Fig. 2, and the corresponding mole-fraction p r o f i l e s for nitrogen and hydrogen are i l l u s t r a t e d i n Fig. 3. Here, the mole-fractions are p lo t t ed as fimctions of ax ia l posi t ion a t various times.

The steady-state chamber pressure w a s taken as 200 psia , the

The r e s u l t s of these calculat ions are shown i n Figs. 1 through Gas temperatures a re p lo t t ed as f'unction of time a t each o f four axial

Generally good agreement between theo re t i ca l

Temperatures a re p lo t t ed as functions of t i m e a t a fixed ax ia l posi t ion i n Fig. 4 f o r cases i n which the i n i t i a l bed temperatures were taken as 530, 950, and 1420 deg R respectively. The comparison between calculated and measured temperature p r o f i l e s i s similar for low and elevated i n i t i a l bed temperature cases.

Additional calculations were made fo r the reactor configuration noted above i n order t o examine the e f f ec t o f pulsed flow on i n i t i a l t rans ien t response. The calculated r e su l t s i l l u s t r a t e d i n Figs. 5 through 11 re fe r t o a reactor operated under pulsed flow conditions a t a steady-state chamber pressure of 260 psia , a steady-state mass flow r a t e of 5.8 lb/ft2-sec, an i n i t i a l chamber pressure of 14.7 ps ia , and an i n i t i a l bed temperature af 530 deg R. Calculations were made f o r t h e f irst two pulses of a duty cycle consisting of a l te rna te on and of f times of 50 msec and 100 msec respectively.

*A p lo t similar t o Fig. 1 w a s included i n Ref. 8; the calculated temperature p r o f i l e s i l l u s t r a t e d i n t h a t p lo t were s l i g h t l y i n e r ror .

10

The temperature i n the i n t e r s t i t i a l phase i s p lo t ted i n Fig. 5 as a fbnction of time a t various axial locat ions i n the react ion chamber. The temperature r i s e s rapidly a f t e r reac tor s tar tup, pa r t i cu la r ly i n the upstream portion of t he chamber. the gas temperature i n the upstream sect ion of the reactor r i s e s extremely rapidly a t f irst because of thermal decomposition of res idua l hydrazine i n t h i s region. In the regions of the reactor downstream of t h e s m a l l c a t a lys t p a r t i c l e s , where the gas temperature i s too low a f t e r 50 msec t o permit s ign i f icant thermal decomposition of hydrazine, the temperature f a l l s due t o heat t r ans fe r from the gas t o the colder ca ta lys t p e l l e t s and t o the chamber w a l l s . The heat gained by the ca ta lys t p e l l e t s i n these regions r e su l t s i n a very small temperature change because of t he la rge mass o f the pa r t i c l e s . temperature i s p lo t ted as a function of time at the same axial locat ions chosen fo r Fig. 5.

When flow in to the reactor i s turned off,

This i s i l l u s t r a t e d i n Fig. 6 where ca t a lys t p a r t i c l e

The rapid pressure buildup and decay resu l t ing from pulse operation of the reactor f o r t h i s case i s shown i n Fig. 7. The species mole-fraction p r o f i l e s associated with t h f s pressure var ia t ion and the temperature d is t r ibu t ions i l l u s t r a t e d i n Figs. 5 and 6 and shown i n Figs. 8 through 11. The var ia t ion of mole-fraction of hydrazine with time a t various a x i a l locat ions i s p lo t t ed i n Fig. 8. thermal decomposition of res idua l hydrazine i n the hot te r upstream regions of the reaction chamber during reactor shutdown as well as the somewhat slower ca t a ly t i c decomposition i n the cooler downstream regions of the reactor . The var ia t ion of mole-fraction of ammonia with time i s i l l u s t r a t e d a t various axial locat ions i n Fig. 9. Following reactor shutdown the residual ammonia near the upstream end,of the reactor decomposes ca ta ly t ic - a l l y i n the hot ca ta lys t pa r t i c l e s . I n the cooler downstream regions, ammonia i s displaced gradually by the nitrogen and hydrogen formed from hydrazine and ammonia decomposition upstream. These decomposition products flow downstream during shutdown as the chamber pressure decays. These processes lead t o the ammonia mole-fraction p ro f i l e s shown i n Fig. 9 and the mole-fraction p ro f i l e s of nitrogen and hydrogen shown i n Figs. 10 and 11 respectively.

This p l o t i l l u s t r a t e s the very rapid

The e f f ec t s of various reactor operating conditions on the t rans ien t

The calculated r e s u l t s r e f e r t o a 23 lb f nominal t h rus t engine 1 . 4 i n . behavior of typ ica l hydrazine reactors are i l l u s t r a t e d i n Figs. 12 through 38. i n diameter with a packed length of 1 . 2 i n . i n to which l i qu id hydrazine i s in jec ted a t a temperature of 530 deg R . A reference case w a s chosen i n which hydrazine in jec t ion w a s taken a t the reactor i n l e t only and i n which the steady-state mass flow r a t e w a s taken as 5.76 lb/ft2-sec (0.04 lb/in2-sec), the in j ec to r pressure as 150 psia , the i n i t i a l chamber pressure as 14.7 psia ,

11

t he i n i t i a l bed temperature as 530 deg R, t he pulse duty cycle as a l te rna t ing 60 msec on and 60 msec o f f , and the ca ta lys t bed configuration as 0.2 in . of 25-30 mesh ca ta lys t p a r t i c l e s followed by 1.0 i n . of 14-18 mesh ca ta lys t p a r t i c l e s . bed #2". bed configuration, and pulse duty cycle were then var ied i n turn and the calculated i n t e r s t i t i a l temperatures a t two axial posi t ions i n the bed were then p lo t t ed as a function of time. The t rans ien t behavior o f the reference case i s i l l u s t r a t e d i n Figs . 12 through 22. Transient i n t e r s t i t i a l tempera- t u r e p r o f i l e s are p lo t ted i n Fig. 12 for two axial posi t ions, one a t the end of the bed and one a t approximately the midpoint of t he bed. i n Fig. 12 are the temperature p r o f i l e s computed a t these same points fo r t h e reactor operating under conditions of continuous ra ther than pulsed flow. The t rans ien t p a r t i c l e temperature p r o f i l e s associated with the i n t e r s t i t i a l temperatures shown i n Fig. 12 are p lo t ted i n Fig. 13, while t he chamber pressure i s p lo t t ed as a function of time i n Fig. 14. The associated mole- f rac t ion p ro f i l e s fo r hydrazine are p lo t t ed i n Figs. 1 5 and 16, fo r ammonia i n Figs. 17 and 18, for nitrogen i n Figs. 19 and 20, and fo r hydrogen i n Figs. 21 and 22.

This bed configuration i s referred t o i n the f igures as "mixed In jec tor pressure, mass flow ra t e , axial in j ec t ion p ro f i l e , ca ta lys t

Also p lo t ted

I n Fig. 23, t rans ien t i n t e r s t i t i a l temperature p r o f i l e s are p lo t ted fo r an in j ec to r pressure of 500 p s i a with a l l other conditions taken as those of t h e reference case. may be noted by comparing Figs. 1 2 and 23. A d i r ec t comparison of e x i t gas temperature p r o f i l e s associated with t h e two d i f fe ren t pressures i s shown i n Fig. 24 fo r the reactor operating under conditions of continuous f l o w .

The very s l i g h t e f f ec t of pressure on t rans ien t response

Transient i n t e r s t i t i a l temperature p ro f i l e s are p lo t t ed fo r steady-state mass flow r a t e s of 1 .44 lb/ft2-sec (0.01 lb/ in . 2- sec) i n Fig. 25 and 14 .4 lb/ft2-sec (0.10 lb/in..2- sec) i n Fig. 26 with all other conditions taken the same as those of t he reference case.* The marked e f f ec t of mass flow r a t e on t r ans i en t response i s fur ther i l l u s t r a t e d i n Fig. 27 f o r a continuous flow system, Here, e x i t gas temperatures are p lo t ted versus time for the three d i f f e ren t steady-state mass flow ra t e s .

The e f f ec t s of d i s t r ibu ted in j ec to r s on t rans ien t temperature p ro f i l e s are i l l u s t r a t e d i n Figs. 28 through 30. of time at the midpoint and a t the end o f the bed i n Figs. 28 and 29 respec- t i v e l y f o r a case i n which 1/4 of the hydrazine i s in jec ted a t the i n l e t and the remaining 3/4 i s in jec ted uniformly over the f i r s t 1/2 in . of the reactor .

Temperature are p lo t t ed as f'unctions

*An in j ec to r pressure of 500 ps ia w a s used i n calculat ions f o r t he high mass flow r a t e case since the high pressure drop associated with t h i s flow r a t e precludes use of the reference in j ec to r pressure.

12

The e x i t gas temperature p r o f i l e s f o r t h i s case and f o r t he reference case of a l l i n l e t in jec t ion a re compared i n Fig. 30 under conditions of continuous flow.

Transient i n t e r s t i t i a l temperature p r o f i l e s a re p lo t t ed f o r d i f fe ren t ca ta lys t bed configurations i n Figs. 31 through 35. Temperature p ro f i l e s associated with beds packed with a l l 25-30 mesh p a r t i c l e s a re shown i n Fig. 31, all 14-18 mesh p a r t i c l e s i n Fig. 32, and the mixture of 25-30 mesh p a r t i c l e s and 1/8 i n . x 1/8 i n . cy l indr ica l p e l l e t s i n Figs. 33 and 34. temperature p r o f i l e s fo r these cases are compared i n Fig. 35 under conditions of continuous flow,

Exit gas

The t rans ien t temperature p ro f i l e s at two axial posi t ions for a pulse duty cycle consis t ing of a l te rna te on and o f f times of 60 msec and 120 msec respectively a re i l l u s t r a t e d i n Fig. 36. The temperature p r o f i l e s associated with a 60 msec/240 msec pulse duty cycle a re shown i n Fig. 37. The e f f ec t s of duty cycle on the t rans ien t response of the e x i t gas temperature are summarized i n Fig. 38.

Additional calculat ions were made t o i l l u s t r a t e t he t rans ien t behavior of a high th rus t hydrazine engine. nominal t h r u s t hydrazine reac tor 4.2 in . i n diameter with a packed length of 1 .0 in . i n t o which l i qu id hydrazine i s in jec ted a t the upstream end of t he reactor only. The ca t a lys t bed packing was taken t o consis t of all 25-30 mesh ca t a lys t pa r t i c l e s ; the steady-state mass flow r a t e was taken as 40.3 lb/ft2-sec, t h e in j ec to r pressure as 1405 ps ia , the i n i t i a l chamber pressure as 0.1 ps ia , ' t he i n i t i a l bed temperature as 530 deg R, and the pulse duty cycle as a l t e r - nating 50 msec on and 250 msec o f f . For this case, i n t e r s t i t i a l temperature, p a r t i c l e temperature, chamber pressure, and the mole-fractiorsof hydrazine, ammonia, nitrogen and hydrogen are p lo t ted as functions of time a t t h e end of the bed i n Figs. 39, 40, 41, 42, 43, 44 and 45 respectively. i l l u s t r a t e t he very rapid t rans ien t response associated with t h i s high flow r a t e system.

The calculations per ta in t o a 600 l b f

These f igures

H910461-38

FEFERENC E S

1. Kesten, A. S. : Analytical Study of Catalyt ic Reactors f o r Hydrazine Decomposition. F i r s t Annual Progress Report, Contract NAS 7-458, May 1967.

United Aircraf t Research Laboratories Report F910461-12,

2. Kesten, A. S . : Analytical Study of Catalyt ic Reactors for Hydrazine Decomposition. Second Annual Progress Report, Contract NAS 7-458, May 1968.

United Aircraf t Research Laboratories Report G910461-24,

3. Smith, E. J . , D. B. Smith, and A. S. Kesten: Analytical Study of Catalyt ic Reactors fo r Hydrazine Decomposition. United Aircraf t Research Laboratories Report G910461-30, Computer Program Manual - One- and Two-Dimensional Steady- S ta te Models, Contract NAS 7-458, August 1968.

4. Smith, D. B . , E. J. Smith, and A. S. Kesten: Analytical Study of Catalyt ic Reactors fo r Hydrazine Decomposition. United Aircraf t Research Laboratories Report H910461-37, Computer Programs Manual - Transient Model, Contract NAS 7-458, May 1969.

5. B i r d , R . B., W. E. Stewart, and E. N . Lightfoot: Transport Phenomena. John Wiley & Sons, Inc . , New York, 1960.

6. Kesten, A. S.: Analytical Study of Catalyt ic Reactors f o r Hydrazine Decomposition - Part I: Steady-State Behavior of Hydrazine Reactors. Proceedings of the Hydrazine Monopropellant Technology Symposium, The Johns Hopkins University Applied Physics Laboratory, Si lver Spring, Maryland, November 1967.

7. Kesten, A. S.: Analytical Study of Catalyt ic Reactors fo r Hydrazine Decomposition - Par t 11: Transient Behavior of Hydrazine Reactors. Proceedings o f the Hydrazine Monopropellant Technology Symposium, The Johns Hopkins University Applied Physics Laboratory, Si lver Spring, Maryland, November 1967.

8. Kesten, A. S. and T. W. Pr ice: Analytical and Experimental Studies of the Transient Behavior of Catalyt ic Reactors fo r Hydrazine Decomposition. Proceedings of t he CPIA 10th Liquid Propulsion Symposium, Las Vegas, Nevada, November 1968.

1 4

H910461- 38

LIST OF SYMBOLS

a Radius of spherical pa r t i c l e , ft

2 Cross-sectional a rea of react ion chamber, f t

T o t a l external surface of ca ta lys t p a r t i c l e per u n i t volume of bed, f t -

Total surface area of chamber walls, f t 2

Reactant concentration i n i n t e r s t i t i a l f l u id , l b / f t 3

Reactant concentration i n gas phase within the porous p a r t i c l e , l b / f t 3

Specific heat of f l u i d i n the i n t e r s t i t i a l phase, Btu/lb- deg R

1 AP

Aw

C i

C P

CP

Average spec i f ic . heat of f l u i d i n the i n t e r s t i t i a l phase, Btu/lb- deg R

Specific heat of ca ta lys t pa r t i c l e , Btu/lb - deg R

CF

cS

CW

dC

Di

DP

F

G

h

h a

'a 1

Specific heat of chamber walls, Btu/lb - deg R

Diameter of react ion chamber, f t

2 Diffusion coef f ic ien t of reactant gas i n the i n t e r s t i t i a l f l u id , f t /sec

Diffusion coef f ic ien t of reactant gas i n the porous p a r t i c l e , f t2/sec

Rate of feed of hydrazine from dis t r ibu ted in j ec to r s i n to the system, lb/f t3- sec

Mass flow r a t e , lb/ft2-sec

Enthalpy, Btu/lb

Heat t r ans fe r coef f ic ien t fo r forced convection between chamber and surrounding atmosphere, Btu/ft2- sec-deg R

Heat t ransfer coef f ic ien t fo r natural convection between chamber and surrounding atmosphere, Btu/ft2- sec-deg R 1.25

Radiation heat t r ans fe r coeff ic ient between chamber and surrounding atmosphere, Btu/ft2- sec- deg R 4

Heat t r ans fe r coef f ic ien t between bulk f lu id and pa r t i c l e s , Btu/ft2-sec-deg R

H910461- 38

H

k

K i

%

C

L

m

M

M

P

W

-

rhet

horn r

R

t

T

vC

wi

z

aP

j3

PJ

Heat t r ans fe r coef f ic ien t between bulk f l u i d and chamber walls, Btu/ft2-sec-deg R

Heat of react ion (negative fo r exothermic reac t ion) , Btu/lb

Mass t r ans fe r coeff ic ient , f t / sec

Thermal conductivity of i n t e r s t i t i a l f l u id , Btu/ft- sec-deg R

Thermal conductivity of t he porous ca ta lys t p a r t i c l e , Btu/ft-sec-deg R

Length of reaction chamber, f t

Thermal mass of chamber walls, lb

Molecular weight, lb / lb mole

Average molecular weight, lb / lb mole

Chamber pressure, p s i a

Rate of (heterogeneous) chemical reaction on the ca ta lys t surfaces, l b / f d - s e c

Rate of (homogeneous) chemical react ion i n the i n t e r s t i t i a l phase, lb/f t3-sec

Gas constant, equals 10.73 ps i a - f t3/ lb mole - deg R

Time, sec

Temperature, deg R

Volume of reactor up t o nozzle throa t exclusive of volume occupied by ca ta lys t pa r t i c l e s , f t 3

Weight f rac t ion of reactant i n i n t e r s t i t i a l phase

Axial distance, f t

In t r apa r t i c l e void f rac t ion

In t e rpa r t i c l e void f rac t ion

Viscosity of i n t e r s t i t i a l f lu id , lb/f t rsec

16

Density of i n t e r s t i t i a l f l u id , l b / f t 3 Pi

PS Bulk density of ca t a lys t p a r t i c l e , l b / f t 3

Subscripts

a Refers t o surrounding atmosphere

F Refers t o feed

i Refers t o i n t e r s t i t i a l phase

P Refers t o gas within the porous ca ta lys t p a r t i c l e

S Refers t o surface of ca ta lys t p a r t i c l e

ss Refers t o steady- s t a t e

W Refers t o chamber w a l l

Superscripts

J Refers t o chemical species

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Attn: Mr. Garland Whisenhunt

Lockheed Missiles and Space Company Attn: Technical Information Center P. 0 . Box 504 Sunnyvale, Cal i fornia 94088


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Attn: Mr. J. D. Goodlette (A-241)

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Attn: M r . A . J. KullaS

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Orlando, F lor ida Box 5837

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Attn: M r . J. Fern 1

McDonnell Ai rcraf t Corporation P. 0. Box 516 Municipal Airport st. Louis, Missouri 63166


1

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Attn: Mr. Y. C . Lee

M c b m e l l Ai rcraf t Corporation P. 0 . Box 516 Municipal Airport S t . Louis, Missouri 63166

Attn: M r . R. A. Herzmark

McDonnell Ai rcraf t Corporation P. 0. Box 516 Municipal Airport St. Louis, Missouri 63166

Attn: Mr. P. Kelley

Rocket Research Corporation 520 South Portland S t r e e t Sea t t le , Washington 98108


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Attn: M r . H. L. Thackwell

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Attn: M r . J . E. Fi tzgerald Rocket Research Corporation 520 South Portland S t r e e t Sea t t le , Washington 98108

Attn: Mr. Foy McCullough, Jr.

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22

~910461- 38

Addressee

Rocket Research Corporation 520 South Portland S t r e e t Sea t t le , Washington 98108

Attn: Mr. Bruce Schmitz

Rocket Research Corporation 520 South Portland St ree t Sea t t le , Washington 98108

Attn: D r . Duane William

Space & Information System Division North American Aviation, Incorporated 12214 Lakewood Boulevard Downey, Cal i fornia 90241


Space & Information Systems Division North American Aviation, Incorporated 12214 Lakewood Boulevard Downey, Cal i fornia 90241

Attn: Mr. H. Storms

Rocketdyne (Library 586-306) North American Aviation, Incorporated 6633 Canoga Avenue Canoga Park, Cal i fornia 91304



Attn: Mr. E. B. Monteath


Attn: Mr. E. V. Ze t t le


Attn: Mr. N . Rodewald

Northrop Space Laboratories 3401 West Broadwsy Hawthorne, Cal i fornia 90250


Northrop Space Laboratories 3401 West Broadway Hawthorne, Cal i fornia 90250

Attn: D r . W i l l i a m Howard

Astro-Electronics Division Radio Corporation of America Princeton, New Jersey 08540


Astro-Electronics Division Radio Corporation of America Princeton, New Jersey 08540

Attn: M r . S. Faimeather

Reaction Motors Division Thiokol Chemical Corporat im Denville, New Jersey 07832


Reaction Motors Division Thiokol Chemical Corporation Denville, New Jersey 07832

Attn: W. Arthur Sherman

Reaction Motors Division Thiokol Chemical Corporation Denville, New Jersey 07832

Attn: M r . Robert Gere

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Republic Aviation Corporation Farmingdale, Long Is land, New York


Republic Aviation Corporation Fsrmingdele, Lang Is land, New York

Attn: Dr . W i l l i a m O'Donnell

Space General Corporation WOO Eaet F l a i r Avenue E l Monte, Cal i fornia 91734


Space General Corporation 9200 East F l a i r Avenue E l Monte, Cal i fornia 91734

Attn: Mr. C. E. Roth

Stanford Research I n s t i t u t e 333 Ravenswood Avenue Menlo Park, Cal i fornia 94025

Attn: Technical Librar ian 1

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Attn: Mr, Lionel Dickinson

TRW System One Space Park Redondo Beach, Cal i fornia 90278


TRW System One Space Park Redondo Beach, Cal i fornia 90278

Attn: Mr. D. Lee

T R W System One Space Park Redondo Beach, Cal i fornia 90278

Attn: Mr. V. Moseley

Tapio Dikision TRW, Incorporated 23555 Euclid Avenue Cleveland, Ohio 44117


Tapco Division TRW, Incorporated 23555 Euclid Avenue Cleveland, Ohio 44117

Attn: Mr. P. T. Angel1

Thiokol Chemical Corporation Huntsvi l le Division Huntsville, Alabama 35807


Thiokol Chemical Corporation Huntsville Division Huntsville, Alebama 3480'7

A t t n : Mr. John Goodloe

United Technology Center 587 Methilda Avenue

Sunnyvale, Cal i fornia 94088 Attn: Technical Librar ian

P. 0. Box 358

United Technology Center 587 Methilda Avenue P. 0. Box 358 Sunnyvale, Cal i fornia 94088

Attn: Mr. B. Adelman

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13910461- 38

Addressee

F lor ida Research & Development Center P r a t t & Whitney Aircraf t United Aircraf t Corporation P. 0 . Box 2691 West Palm Beach, F lor ida 33402


F lor ida Research & Development Center P r a t t B Whitney Aircraf t United Aircraf t Corporation P. 0. BOX 2691 West Palm Beach, F lor ida 33402

Attn: Mr. R . J. Coar

Vickers Incorporated

Troy, Michigan BOX 302


Sunstrand Aviation 2421 11th S t r e e t Rocirford, I l l i n o i s 61101


Sunstrand Aviation 2421 11th S t r e e t Rockford, I l l i n o i s 61101

Attn: M r . R. W. Re.ynolds

Hamilton Standard Division United Aircraf t Corporation Windsor Locks, Connecticut 06096


Hamilton Standard Division United Aircraf t Corporation Windsor Locks, Connecticut 06096

Attn: Mr. R. Hatch

Technical Library A i r Research Manufacturing Company 9851 Sepulveda Boulevard Los Angeles, California 90009


A i r Research Manufacturing Company 9851 Sepulveda Boulevard Los Angeles, Cal i fornia 90009

Attn: Mr. C . S. Coe

A i r Research Manufacturing Company 9851 Sepulveda Boulevard Los Angeles, Cal i fornia 90009

Attn: M r . A. C. Standiffe

Shel l Development Company 1400 53rd S t r e e t Emeryville, Cal i fornia 94608



Attn: D r . H. Voge


Attn: D r . T. J. Jennings

Brooklyn Polytechnic I n s t i t u t e Department of Chemical Engineering 333 Jay S t r e e t Brooklyn, New York 11201


Copiea Addreeeee

1 Brooklyn Polytechnic I n s t i t u t e Lhpartment of Chemical Engineering 333 Jay S t r e e t Brooklyn, New York 11201

Attn: Prof. I. Mil ler

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H9 1046 1-38 COMPARISON OF THEORETICAL AND EXPERIMENTAL

TRANSIENT TEMPERATURE PROFILES

I

FIG. 1

I I

STEADY-STATE CHAMBER PRESSURE = 200 PSIA STEADY-STATE MASS FLOW R A T E = 6.5 L B / F T - SEC

C A T A L Y S T B E D CONFIGURATION: M I X E D B E D # 1 (SEE T E X T )

SEE T E X T FOR ADDIT IONAL R E A C T O R PARAMETERS I N I T I A L B E D T E M P E R A T U R E = 530 DEG R

2100

(A) AXIAL POSITION = 0.08 F T

'

21 00

A 5 e 2 c3 1700

I - P E l

I - K

w w

z .- -I- : w' 1300 2 2 sal w n L w 900 I-

500

T H E 0 RE T I C At. ----- - -EXPERIMENTAL

0 1 2 3

TIME, t - SEC

(C) AXIAL POSITION = 0.17 F T

2100 I T H E O R E T I C A L

0 1 2 3

TIME, t - SEC

2100

1700

1300

900

500 0 1 2 3

TIME, t - SEC

(D) AXIAL POSITION = 0.25 F T ~

T H E O R E T I C A L

1700

1300

900

500

0 1 2 3

TIME, t - SEC

H9 1046 1-38 FIG. 2

c3 W n 0 M v,

I1 w K 3 I-

K W

=E W I-

W

A

I- Z

a

n

n m

a - - -

h! 0

c

0 -! 0

3SVHd l V l l I l S Z l 3 l N I N I VINOWWV d 0 N0113V'LId-310W

v! 0

? 0

7

0

3SVHd l V I l I l S Z l 3 1 N I NI 3NIZV'LIaAH A0 N0113V'LIA-310W

0

0

I- L

I N

W- U Z 4 I- 2 n J 4 z 4

+ U I N

W' U Z 4 5 - n 4 4 X 4

-

H9 10461 -38 FIG. 3

z W c3 0 a ). I

z e

n

n

z W

L O O m

v,

U w

I

I- LL \

J

vl

cv

m

2 I1

UI I- d e

[r: W

2 a L U W I- d

I 5;

U c W U vl u m P Y) C

8 C

1 I I I 1 I 1 0

l-? 0

7

0

3SVHd l V l l l l S Z I 3 1 N I NI N33011aAH 40 N0113VZI4-31OW

0

5;

U W vl

U w vl m Y)

8

0 9 0

1 0 2 -

0

3SVHd l V l l l l S Z I 3 1 N I NI N3301111N 40 N0113VZI3-310W

H910461-38 FIG. 4

0 0 !2

0 0 m F

0 0 OI

0 0 v)

0 0 ' 0

h( E 2 0 0 2

0 0 OI

0 0 v)

\\ \ 0 0

cv F

0 0 m - 0

0 OI

2l 33a - '1 '3SVHd

1 V l l I lS2 l I I lN I NI 32lnlV2I3dW3 1

0 0 v)

U w v)

I + W

I- r

W W v)

I t

ui r I-

H9 10461 -38 FIG. 5

VARIATION OF INTERSTITIAL TEMPERATURE WITH TIME AT VARIOUS AXIAL POSITIONS

STEADY-STATE CHAMBER PRESSURE = 260 PSIA S T E A D Y - S T A T E MASS FLOW R A T E = 5.8 L B / F T 2 - SEC

C A T A L Y S T B E D CONFIGURATION: M I X E D B E D # 1 (SEE T E X T ) SEE T E X T F O R A D D I T I O N A L R E A C T O R PARAMETERS

2000

1800

1600

1400

1200

1000

800

600

400

200

L 0.010 F T

A X I A L POSITION, z

0,010

I

0.052

/

0.052 F T

0.140 F T

0.308 F T

F T

0.140 F T

/

/ OS3O8 F T

I 1 I ON I R E A C T O R O F F

I I REACTOR ON

1 1 1 I 1

0 40 80 120 160 200 240

TIME, t - MILLISECONDS

H910461-38 FIG. 6

K

s n I n

I-

A u I- K 4 L

W'

-

z

a I k

* A 4 I-

u I

3 w K a I-

w 0. I W c

a

2200

2000

1800

1600

1400

1200

1000

800

600

400

VARIATION OF CATALYST PARTICLE TEMPERATURE WITH TIME A T VARIOUS AXIAL POSITIONS

STEADY-STATE MASS FLOW R A T E = 5.8 L B / F T ~ - SEC

STEADY-STATE CHAMBER PRESSURE = 260 P Y A


SEE T E X T FOR ADDITIOI4AL R E A C T O R PARAMETERS

A X I A L POSITION, z =

0.010 F T

0.052 F T

0.140 F T

0.308 F T

I REACTOR O N I I

I R E A C T O R O F F I

R E A C T O R O N I

0 40 80 120 160 200 240


H910461-38 FIG. 7 VARIATION OF CHAMBER PRESSURE WITH TIME

STEADY - S T A T E CHAMBER PRESSURE = 260 PSlA S T E A D Y - S T A T E MASS FLOW R A T E = 5.8 L B / F T 2 - SEC C A T A L Y S T B E D CONFIGURATION: M I X E D B E D # 1 (SEE T E X T )

SEE T E X T FOR A D D I T I O N A L R E A C T O R PARAMETERS

200

180

160

140

120

100

80

60

40

20

0

r

I I ’ REACTOR ON I I R E A C T O R O F F REACTOR ON I

0 40 80 120 160 20 0 2 40


H910461-38

0.6

0.5

0-4

0.3

0.2

0.1

0

VARIATION OF MOLE-FRACTION OF HYDRAZINE WITH TIME AT VARIOUS AXIAL POSITIONS

STEADY-STATE CHAMBER PRESSURE = 260 PSIA

S T E A D Y - S T A T E MASS FLOW R A T E = 5.8 L B / F T z - SEC

C A T A L Y S T B E D CONFIGURATION: M I X E D B E D t# 1 (SEE T E X T )

SEE T E X T FOR A D D I T I O N A L REACTOR PARAMETERS

I I I R E A C T O R O N I REACTOR O F F I R E A C T O R ON I

I I I

iL POSITION, Z = - 0.010 FT

I I

0 40 80 120 160 200 240


H9 1046 1 - 38 FIG. 9

0 e6

0.5

0.4

0.3

0.2

0.1

0

VARIATION OF MOLE-FRACTION OF AMMONIA WITH TIME A T VARIOUS AXIAL POSITIONS

STEADY-STATE CHAMBER PRESSURE = 260 PSlA

2 STEADY-STATE MASS FLOW R A T E = 5.8 L B / F T - SEC


SEE T E X T FOR ADDIT IONAL REACTOR PARAMETERS

I I REACTOR ON I R E A C T O R O F F I R E A C T O R ON I

I I I

L 0.010 F T

0.308 F T 0.140 F T 0.052 F T 0.010 F T

0 40 80 120 160 200 240


H910461-38 FIG. 10

0.6

0.5

0.4

0.3

0.2

0.1

0

VARIATION OF MOLE-FRACTION OF NITROGEN WITH TIME AT VARIOUS AXIAL POSITIONS

S T E A D Y - S T A T E CHAMBER PRESSURE = 260 PSlA STEADY-STATE MASS FLOW RATE = 5.8 L B / F T ~ - SEC

C A T A L Y S T B E D C O N F I G U R A T I O N : M I X E D B E D # 1 (SEE T E X T ) SEE T E X T FOR A D D I T I O N A L R E A C T O R PARAMETERS

A X I A L POSITION, Z =

r\ 0.052 F T

1 I

I I I I I I I

I REACTOR O N I I R E A C T O R O F F REACTOR ON I

0 40 80 120 160 200 240


H910461-38 FIG. 1 1

0 e9

0.8

0 a 7 w

I L J

2

0.6 c 5 K W I- Z -

0.5 z Z W c3 0 K

I LL 0 Z 0

0.4

- 0,3

4 oi U I

W J 0 L 0.2

0.1

0

VARIATION OF MOL€-FRACTION OF HYDROGEN WITH TIME A T VARIOUS AXIAL POSITIONS


S T E A D Y - S T A T E CHAMBER PRESSURE = 260 PSIA


SEE T E X T FOR ADDIT IONAL REACTOR P A R A M E T E R S

0.052 F T ~.

0.140 F T

0.308 F T 0.140 F T 0.052 F T 0.010 F T

A X I A L P O S I T I O N , z =

0.308 F T 0.140 F T 0.052 F T

0.010 F T

R E A C T O R O N I R E A C T O R O F F I REACTOR ON I I I 1

I I I I I

0 40 80 120 160 200 240


H9 10461 -38 FIG. 12

2200

2000

1800

K 0 W n

I 1600 6- uii 2 I a A 1400 4 c I- v) K W

-

g 1200 - W K 3 2 1000 w

800

600

TRANSIENT INTERSTITIAL TEMPERATURE PROFILES FOR THE REFERENCE OPERATING CONDITIONS

INJECTOR PRESSURE = 150 PSlA

STEADY-STATE MASS FLOW R A T E = 5.76 L B / F T - SEC

CATALYST B E D CONFIGURATION: MIXED B E D # 2 (SEE T E X T )

SEE T E X T FOR ADDITIONAL REACTOR PARAMETERS

REACTOR STATUS

I N 'OFFION'OFF'ON 'OF ON'OF?&lOF ON'OFF'ON'OFF'ON 'OFF'ON'OFFl ON !OFF'ONlOF?ONlOFF'ON ' O F F i - ~ N ~ F ~ O ~ I I I I < I 1 1 . 1 1 I I I I l l I I I I I 1 I I I I I I

I I I I I I

z = 0.052 FT I---

L

L

I I

I I I I :::: P 1

I I / I

REPRESENT CONTINUOUS OPERATION

I I I L A 40 0 0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H9 10461 -38

-

FIG. 13

t 2000 1-

-

1800- c3 W

I n

n -

1600- W'

u

' 1400 -

J

I- K

-

I- v) 2- 4

I- d: a

" 1200- z t -

-

z

3 W

3 I-

d

I-

TRANSIENT PARTICLE TEMPERATURE PROF1 LES FOR THE REFERENCE OPERATING CONDITIONS



CATALYST B E D CONFIGURATION: MIXED B E D # 2 (SEE T E X T ) SEE T E X T FOR ADDITIONAL REACTOR PARAMETERS

DASHED CURVES REPRESENT CON T I NUOU S 0 PERATION

H9 1046 1-38 FIG. 14

TRANSIENT CHAMBER PRESSURE PROFILE FOR THE

REFERENCE OPERATING CONDITIONS


STEADY-STATE MASS FLOW RATE = 5.76 L B / F T 2 - SEC

CATALYST BED CONFIGURATION: MIXED BED # 2(SEE T E X T )


REACTOR STATUS

0 N ~ F F ~ O N ~ O F ; r O N ~ O F F ~ O N I O F F ~ ~ O N I O F ; O ~ ~ ~ ~ ~ N ~ F F ~ O N ( ~ ~ I I 1 140

120

100 1 n

n w- 80

VI

I

K 2 Y, v) W K

K 6o W

n

: I u

40

20

0

DASHED CURVE REPRESENTS I CONTINOUS OPERATION i.

L

c

f f

\ L L L

0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H9 10461-38 FIG. 15

TRANSIENT PROFILE OF MOLE-FRACTION OF HYDRAZINE FOR THE REFERENCE OPERATING CONDITIONS

INJECTOR PRESSURE = 150 PSIA

STEADY-STATE MASS FLOW RATE = 5.76 LB/FT - SEC

CATALYST BED CONFIGURATION: MIXED B E D # 2 (SEE T E X T )


0*0510N;,FF10N I --I--- REACTOR STATUS

W v) F F F l O N b F F l O N IOFFjON (OFFION I 0 F F ; O N ~ O F F ~ O N ~ O F F ~ O N ~ 0 F F ~ O N ~ O F ~ O N ~ 0 F F ~ O N 1OFF;ON , O F F ~ O N ~ O F F ; O N 1OFI

LL 0 Z

I-

ai LL I

w

z y 0.0

DASHED CURVE REPRESENTS CON T I NUOU S OP ERATl ON

AXIAL POSITION, z = 0.052 F T J

“0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1-

1.8 TIME, t - SECONDS

H910461-38

i 0 L

OO 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

FIG. 16

w 0.05

I n -I 4 E 0.04 I- v) oi W I-

2

z 0.03

W Z N U oi

- n

0.02 LL 0 z I-

oi LL

I W

y 0.01

TRANSIENT PROFILE OF MOLE-FRACTION OF HYDRAZINE FOR THE REFERENCE OPERATING CONDITIONS



CATALYST B E D CONFIGURATION: M I X E D BED # 2 (SEE T E X T )


REACTOR STATUS ONlOFFlON IOFF'ON1OFFIONIOFFION 'OFF' O N ' O F F ~ O N ~ F F l ON'OFF~ON 'OFFlON ~ O F F ~ O N ' O F F ~ O N ~ O F F ~ O N ~ O F ~ ~ O N ~ O F ~ O N I O F f -T-

I I I I I I I I I I I I 1 I I

AXIAL POSITION, z=.lOO F T I DASHED CURVE REPRESENTS

CONTINUOUS OPERATION

H9 1046 1-38 FIG. 17

0.7

0.6 w v) 4 I n -I 5 0.5 c s oi w c ' 0.4 3 5 z s 4 0.3 LL 0 z c u E U I

w -I 0 z:

s 4 0.2

0.1

TRANSIENT PROFILE OF MOLE-FRACTION OF AMMONIA FOR THE REFERENCE OPERATING CONDITIONS





REACTOR STATUS

I N k F F I O N )FFiON ~ F F ~ O N ~ O F F ~ O N ( O F F I 0 N b F F l O N bF(ON!OFF/ON b F ( O N b F ( O N ~ F F l 0 N ~ F F ; O N f i F F ~ O N kFF!ONlOFf I

DASHED CURVE REPRESENTS


0 0 0.2 0.4 0.6

1 I AXIAL POSITION, z=0.052 F T I

I 0.8 1.0

TIME, t - SECONDS

1 1.2 : 1.4 1.6 1.8

H9 10461-38 FIG. 18

0.7

0.6 W UJ

I p. -I

a

a

5; p 0.5 - Di W I- z z, a

0.4

- z 0 L ' 0.3 LL 0 z I- W

z 2 0.2 LL

I W -I 0 L

0.1

0

TRANSIENT PROFILE OF MOLE-FRACTION OF AMMONIA FOR THE REFERENCE OPERATING CONDITIONS



CATALYST BED CONFIGURATION: MIXED BED # 2 (SEE T E X T )


I I I I I I I

0 0.2 0.4 0.6 0.8



1 AXIAL POSITION, z = 0.100 F T 1

1.0 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H91046 1-38 FIG. 19

TRANSIENT PROFILE OF MOLE-FRACTION OF NITROGEN FOR THE REFERENCE OPERATING CONDITIONS


STEADY-STATE M A S S FLOW R A T E = 5.76 L B / F T ~ - SEC

CATALYST B E D CONFIGURATION: MIXED BED # 2 (SEE T E X T )


REACTOR STATUS 0.6

ON j o ~ F; ON ;OF FI ON ~ F F ; ON ;OFF: ON FF F; ON ;OFF] ON !OFF; ON ~ F F ' ON IOF F' ON ;OF FI ON 'OFF' ON PF F\ ON 'OFF[ ON OF FI 03 I l l 1 1 1 l I I l l

W

2 0.5

9 k

E 0.4

3 I:

0 0.3

I- v)

+

Z W

0 K

Z L 0 z 0.2 e l- V 4 K L

I

J 0 L

W 0.1

1 DASHED CURVE REPRESENTS CONTINUOUS OPERATION

1 AXIAL POSITION, z=0.052 F T I ___

n I I I I 1 I I I I I 1 I I I I I - "0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H9 1046 1-38

O O 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8

FIG. 20

0.6

W

2 0.5

L -I U i= - 5;

f z o 0.3

E

0.4 c

Z W

0 ai

Z L 0 z 0.2 z I- W 4 ai L I

w 0.1 J 0 =E

TRANSIENT PROFILE OF MOLE-FRACTION OF NITROGEN FOR THE REFERENCE OPERATING CONDITIONS


STEADY -STATE MASS FLOW R A T E = 5.76 L B / F T - SEC


SEE T E X T F O R A D D T I O N A L REACTOR PARAMETERS

REACTOR STATUS

ON ‘OFF‘ ON ‘OFF: ON ‘OFF/ ON b F F l ON b F F \ ON ‘OFF/ ON +FF! ON k F F l ON :OF( O N /OFF/ ON [OF$ ON kFFlON I ‘ O ~ ~ N w o N ~ l I 1 I l l I I I

DASHED CURVE REPRESENTS r-. CON T I NU OU S 0 P ERATl ON

AXIAL POSITION, z=O,lOo F T

H9 1046 1-38 FIG. 21

0.9

0.8

0.7 v) a I Q

-I a p 0.6

5 Q! W c f

0.5 - Z w c3 0 K

I U 0 z 6, l- u 0.3 U bi LL I

W J 0

n * 0.4

L 0.2

0.1

TRANSIENT PROFILE OF MOLE-FRACTION OF HYDROGEN FOR THE REFERENCE OPERATING CONDITIONS

INJECTOR PRESSURE = 150 P Y A


CATALYST BED CONFIGURATION: MIXED BED # 2 ( SEE TEXT)


REACTOR STATUS

1 ~ N P F F I O N ~ O F F I O N I O F F ~ O N 7 1 ~ ~ ~ , 1 7 ON , O F F ~ O N ~ O F ~ O N ~ O F F ~ O N ~ O F F ] O N ~ O F F ~ O N , O F F , O N ~ O F F ~ O N ~ O F F ~ O N ~ O F F , -7-11- -T O N ~ O F F ~ T---r O N ~ O F F - 1 -

I

?-

I Z P O S I T I O N , z = 0,052 F T I DASHED CURVE REPRESENTS


0 0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H9 1046 1-38 FIG. 22

0.9

0.8

W 0.7 2

a I L

- I- F 0.6 VI E W I- E E 0.5 Z W CJ

E! n

I 0.4 > L 0 Z 0 I- U

L I

W -I 0 I

-

2 0.3

0.2

0.1

0

TRANSIENT PROFILE OF MOLE-FRACTION OF HYDROGEN FOR THE REFERENCE OPERATING CONDITIONS


STEADYSTATEMASS FLOW RATE = 5-76 L B I F T ~ - S E C

CATALYST BED CONFIGURATION: MIXED BED # 2 (SEE TEXT)


c

r

j I

~ X I A L J POSITION, ~ o.100 FT __ - - __

-7 ___ - - __

DASHED CURVED REPRESENTS

CONTINUOUS OPERATION 1 ~- - -

0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8 TIME, t- SECONDS

H9 10461-38

i 1200- K 3 I- K a

TRANSIENT INTERSTITIAL TEMPERATURE PROFILES

I - 1

FIG. 23

I

FOR AN INJECTOR PRESSURE OF 500 PSlA

I I I I I I I I I I I I I

STEADY-STATE M A S S FLOW RATE = 5.76 L B / F T ~ - S E C

CATALYST B E D CONFIGURATION: MIXED BED # 2 ( S E E TEXT)

SEE T E X T FOR FOR ADDITIONAL REACTOR PARAMETERS

T _ _ REACTOR STATUS

ON IOFFlON ;OF( ON PFFl ON :OF< ON ;OF( ON b F 4 ONiOFF1ON ;OFF: ON \OFF! ON (OFF! ONiOF4 ON10F4 ON !OFf

I I I

I I Y izi

DASHED CURVES REPRESENT


H9 10461 -38 FIG. 24 COMPARISON OF TRANSIENT INTERSTITIAL TEMPERATURE PROFILES FOR TWO

INJECTOR PRESSURES IN A CONTINUOUS FLOW SYSTEM

I I I I I I I I I

STEADY-STATE M A S S FLOW R A T E = 5.76 L B / F T ~ - SEC

CATALYST BED CONFIGURATION: MIXED BED # 2 ( S E E T E X T )

SEE T E X T FOR ADDTITIONAL REACTOR PARAMETERS

I

240 0

2200

BOO

CI 1800 n

I=

W' 2 1600

W

I

I 0. J 4 I-

5 1400

I E

- K W I-

; 1200

d 5 1000

3 I-

W n.

I-

800

600

AXIAL POSITION = 0.100 F T I - -1

400 0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8

T1ME.t - SECONDS

TRANSIENT INTERSTITIAL TEMPERATURE PROFILES FOR A STEADY-STATE MASS FLOW RATE OF 1.44 LB/FT*-SEC

H 9 1 046 1 - 38 FIG. 25

INJECTOR PRESSURE = 150 PSIA CATALYST BED CONFIGURATION: MIXED BED # 2 ( S E E T E X T )


H91046 1-38

2400

2200

2000

K

W

I

F- W' 2 1600

n

0 1800 n

I

a - I-

v) ni W I-

Z

oi 3 I- 4 K W Q

W I-

F 1400

z 1200

1000

800

60L

TRANSIENT INTERSTITIAL TEMPERATURE PROFILES FOR A STEADY-STATE MASS FLOW RATE OF 14.4 LB/FT * - SEC

fNJECTOR PRESSURE = 150 PSIA CATALYST BED CONFIGURATION: MIXED BED # 2 (SEE T E X T )


FIG. 26

z = 0.100 F T

l-----l DASHED CURVES REPRESENT


I c

I I I 1 I I I I I 40 0 I I I I I 0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H910461-3e FIG. 27 COMPARISON OF TRANS! ENT INTERSTITIAL TEMPERATURE PROFILES FOR VARIOUS

STEADY-STATE MASS FLOW RATES IN A CONTINUOUS FLOW SYSTEM


CATALYST BED CONFIGURATION: MIXED BED # 2 (SEE TEXT)


240 0

2200

2000

w 1800 c3 W n I

&- wi 1600

2 I L J 4 F 1400 I- Lo E w I-

-

f z - 1200 w w 3 I- < w

5 W I-

E 1000

800

600

MASS FLOW R A T E ( L B . / F T ~ ' - SEC) =

14.4

i AXIAL POSITION, L = 0.100FT

400 0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8

TIME. t - SECONDS

H9 1046 1 -38

I I I I I I I I I I I I

FIG. 28

I

2400

2200

2000

K

2 1800 P I

I- .-

W' 1600

I 0. -I 4 I- 5 1400

E z

- K W I-

1200 3 I- U K W R

I- 1000

800

600

TRANSIENT 1NTERSTlTlAL TEMPERATURE PROFILE FOR A BURIED INJECTOR CONFIGURATION


CATALYST B E D CONFIGURATION: MIXED B E D # 2 ( S E E T E X T )


REACTOR STATUS

~ N ~ O F F I O N ~ O F F I O N ~ O F F I O N ~ O F F ~ O N I I I I I I I I ;OFFION I ~ ~ F F I O N ~ O F F ~ O N ~ O F F I O N ~ O F F ~ O N ~ O F ~ O N ~ O F F ~ O N ~ O F F ~ O N ~ ~ F F I O N I l l I I ~OFF~ONIC

1. 44

'0 0.04167 0.1 z

AX1 AL PO SI TION, z = 0.052 F T

DASHED CURVE REPRESENTS CON TIN UO U S

400 0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H9 1046 1-38 FIG. 29 TRANSIENT INTERSTITIAL TEMPERATURE PROFILE FOR A BURIED INJECTOR CONFIGURATION

I I I

2400

2 200

2000

OL

z: 1800 P

I

I- .-

2 1600 4 I n. J 4 I- F 1400 - v) K W I- Z - E w 1200 K 3 I- U K w n 5 1000 I-

800

600

400 I I I I I I I I

INJECTOR PRESSURE = 150 PSlA CATALYST BED CONFIGURATION: MI XED B E D # 2 (SEE T E X T )


0 /

/ /

------------- -?-

G5'76v, 1.44 0

0 0.4167 , I

z = O . I O O FT

DASHED CURVE REP RESENTS CONTINUOUS OPERATION

0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

TIME, t - SECONDS

FIG. 30 H910461-35 COMPARISON OF TRANSIENT INTERSTITIAL TEMPERATURE PROFILES FOR TWO INJECTION

CONFIGURATIONS IN A CONTINUOUS FLOW SYSTEM


CATALYST BED CONFIGURATION: M I X E D BED # 2 ( SEE T E X T )


2mc

2200

2000

E

W

I

(3 1800 n

g- W'

u 1600 v)

I CL. J U i= 5 1400 o? W I- Z

Z - -

1200 3 I-

w L

I-

2

5 loot

sot

60(

40 C

AXIAL POSITION, z=O.IOO FT i - L

G 1.44 u

0 0.04167 - 1 Z @

5.76

1

0 1 0 .1

Z

0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1 ,

TIME, t - SECONDS

3

H9 10461 -38 FIG. 31 TRANSIENT INTERSTITIAL TEMPERATURE PROFILES FOR A CATALYST BED

PACKED WITH ALL 25-30 MESH PARTICLES

INJECTOR PRESSURE = 150 PSIA STEADY-STATE MASS FLOW RATE = 5.76 L0/FT2 - SEC


REACTOR STATUS

ON iOF<ON l O F { O W / O F < O N ' p F F ~ O N b F F l O N ;:,FFION ~ F F \ O N ~ O F ~ O N i O F d O N ~ O F F I O N ~ O F F ~ O N , O F F i -r-r--r-r-r--T O N I O F ~ O N ( O F ~ ( O N --r I lOFF - r 1

2400 i

2000

- I 1800 n

I

I-

W

I

-I

.-

2 1600 n

a k 5 1400'

E I i

I - c oi W I-

; 1200 t 3 I-

oi W

a

n 3 1000 I-

800

/

600 p-/J

0,100 FT

DASHED CURVES REP RESENT CON TIN U OU S OPERATION

TRANSIENT INTERSTITIAL TEMPERATURE PROFILES H9 10461 -38

FOR A CATALYST BED PACKED WITH ALL 14-18 MESH PARTICLES

2400

2200

2000

E

1800 n I

e .- W‘

4 1600 n

5

VI

I

-I

c c

W I-

- g 1400

f f

1200 3 c Q K W n x ; 1000

800

60 0

400


STEADY-STATE MASS FLOW RATE = 5.76 L 0 / F T 2 - SEC


FIG. 32

REACTOR STATUS

)N PFF; ON \OFF; ON PFF~ ON PFF~ ON :OFF: ON ;OFF; O N ~ O F F ~ ON ~ F F ; ON ;OFF] ON ;OF( ON ;OFF{ O N ;OF+ ON ;OF(

1 I I I I I I I

-------

I I

I I I /v DASHED CURVES

REPRESENT CONTINUOUS OPERATION I II

0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H910461-38

-I 4 k 5 1400

f 3

K W I-

1200 3 I- U LK W n 3 1000 I-

800

600

TRANSIENT INTERSTlTlAL TEMPERATURE PROFILE FOR THE “MIXED BED #I” CATALYST BED CONFIGURATION

/ -

- / - / -

-

-

--

I -



S E E T E X T FOR ADDITIONAL REACTOR PARAMETERS

I I I I I I

FIG. 33

I I I

F 2200

2000

/ t K

2 1800 n

/ /

c

0 /

1: I I AXIAL POSITION. z = 0.052 F T I

DASHED CURVE REPRESENTS CONTINUOUS OPERATION

0 0.2 0.4 0.6 o .a 1 .o 1.2 1.4 1.6 1 .8

TIME, t - SECONDS

H910461-38

I I I I I I

2400

2200

2000

K

1800 P I

F .-

w- 2 1600 r n

4 -I

5; 1400

E

K W I-

Z - ; 1200 3 I- U K W n z 1000 I-

800

600

40 0 I I I I I I

TRANSIENT INTERSTITIAL TEMPERATURE PROFILE FOR THE “MIXED BED #1” CATALYST BED CONFIGURATION


STEADY-STATE MASS FLOW RATE= 5.76 L B / F T 2 - SEC


FIG. 34

REACTOR STATUS

I N ~ F < O N ~ O F F ~ O N ~ F F I O N [ O F F ~ O N ~ F ( ON ~ F F I O N ~ O F ( O N ~ O F $ ONIOFF]ON ( O F { O N ~ O F F ( O N ~ O F { O N ~ O F { O N /OF+ O N ~ O

- - - - - / - - I I

0 /

/ - /

/ /

/ /

- / /

/ /

c

/ /

/

0

2 1


I I

I AXIAL POSIT ION, r= 0.100 F T I

0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H910461-38 FIG. 35 COMPARISON OF TRANSIENT INTERSTITIAL TEMPERATURE PROFILES

FOR VARIOUS BED CONFIGURATIONS IN A CONTINUOUS FLOW SYSTEM




2400

2200

K 2000

n c3 W

I

I- .-

1800 w- 2 I L -I 4 F 1600 - t;;

f z 1400

K W I-

- w K 3 I- 4 K

120c 3 I-

1 ooc

800

600

400

1 . - _ .

0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8 TIME, t - SECONDS

H910461-38 FIG. 36

2400

2200

2000

4Y 1800

n I

I- .-

1600 U I 0,

-I U t 5; 1400

z f w 1200

-

4Y w I-

4Y 3 I- U 4Y W

$ l0OC I-

800

600

400

TRANSIENT INTERSTITIAL TEMPERATURE PROFILES FOR 60 msec/l20 msec PULSE DUTY CYCLE

INJECTOR PRESSURE = 150 PSIA STEADY-STATE M A S S FLOW RATE = 5.76 L B / F T ~ - SEC

CATALYST BED CONFIGURATION: MIXED BED # 2 (SEE T E X T ) SEE T E X T FOR ADDITIONAL REACTOR PARAMETERS

-~r ~ - - - ~ o F F - - REACTOR STATUS ' OFF I O N ; OFF ; O N ' OFF ;ON! OFF : O N ; OFF I O N ; OFF ; O N ; OFF I O N ; OFF I O N , OFF , O N , I I

I I I I I I I I

0.100 F T

/ I

0.052 F T

0.100 F T

DASHED CURVES REPRESENT

CONTINUOU S OPERATION

0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H9 1046 1 -38 FIG. 37 TRANSIENT INTERSTITIAL TEMPERATURE PROFILES

FOR 60 msed 240msec PULSE DUTY CYCLE

INJECTOR PRESSURE = 150 PSlA STEADY-STATE MASS FLOW RATE = 5.76 L B / F T - SEC

CATALYST B E D CONFIGURATION: MIXED BED # 2 (SEE T E X T ) SEE T E X T FOR ADDITIONAL REACTOR PARAMETERS

REACTOR STATUS

)NI I OFF ; O N ; OFF ; O N ; OFF I O N : OFF I ON; 2400

2200

2000

Di

$ 1800 n

I

I- .-

W' 2 1600 I Q -I

I- 4 -

1400 E W I- z z w 1200 Di 3 I- 4 ai W Q

I- z 1000

800

600

40 0

OFF I

I

/ I

/ /

/ L 1 I

I I /

I I

I I

I I

I I I I I

0.052 F T

L

i 0.100 F T I

I I

r - 7 I DASHED CURVES

REPRESENT CONTINUOUS OPERATION

0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8

TIME, t - SECONDS

COMPARISON OF TRANSIENT INTERSTITIAL TEMPERATURE PROFILES FOR VARIOUS PULSE DUTY CYCLES

H910461-38

2400

220c

200(

Qi

E 180( n I

I- .-

W' 2 1600 I L A

+ 9

5; 140(

f z

- Qi W I-

1200 2 I- U Qi w n

1000 I-

800

600

400



CATALYST B E D CONFIGURATION: MIXED B E D !4 2 (SEE T E X T )


FIG. 38

@ CONTINUOUS OPERATION

@ DUTY C Y C L E : 60 msec ON, 60 msec O F F

0 DUTY CYCLE : 60 msec ON, 120 msec O F F @ DUTY C Y C L E : 60 msecON. 240 msec O F F

-_ -

&.P- / 0 / /e---- /=-

'6 / .I

/ /

I ' I'

. 1 I

I I

I . . . -

I I

I I AXIAL POSITION

Z = 0.100 F T ,

0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H9 10461 -38 FIG. 39 TRANS1 ENT INTERSTITIAL TEMPERATURE PROFILE FOR A HIGH THRUST ENGINE

INJECTOR PRESSURE = 1405 PSIA STEADY-STATE MASS FLOW R A T E = 40.3 L B / F T ~ - SEC

C A T A L Y S T B E D CONFIGURATION: A L L 25-30 MESH PARTICLES SEE T E X T FOR ADDITIONAL REACTOR PARAMETERS

240(

220c

2000

y 180C n

I=

W'

4 160C

I

v)

I 0, 1 9 k I-

W I-

1400

z z

120c 3 I-

W R

I-

d 5 1000

800

600

400

-r __ ~- REACTOR STATUS -

OFF ION; OFF ;ON; OFF :ON/ OFF l O N l OFF (ON1 OFF 1

. I I

I

DASHED CURVE REPRESENTS CON TI NUOU S 0 P E R AT1 ON

AXIAL POSITION, z = 0.084 F T

0 0.1 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1 .a TIME, t - SECONDS

H910461-38 FIG. 40 TRANSIENT PARTICLE TEMPERATURE PROFILE FOR A HIGH THRUST ENGINE

I I I I I I I


STEADY-STATE MASS FLOW R A T E = 40.3 L B / F T ~ - S E C CATALYST BED CONFIGURATION: A L L 25-30 MESH PARTICLES


I I

2400

2200

2000

K c3

1800 I P

I-

W'

6 1600 I- K 4 CL

-

t;; 5 1400 U I- 4 u f - 1200 5 w K 3 I- U

L

I-

1000

5

800

600

400

REACTOR STATUS

I N I OFF lONl OFF lON l OFF I ON1 OFF JON1 OFF ION1 O F F I I I I I ---1---


CON TIN UOU S 0 P E RAT ION

I I AXIAL POSITION, z = 0.084 F T

H910461-38 FIG. 41 TRANSIENT CHAMBER PRESSURE PROFILE FOR A HIGH THRUST ENGINE

700 I

L L

Q: 1 600 0,

I , n

W'

2 500 -- K l v) u K L K u rn 5 400 I u

-

300

i


STEADY-STATE MASS FLOW RATE = 40.3 L B / F T - SEC

C A T A L Y S T B E D CONFIGURATION: A L L 25-30 MESH PARTICLES


.

c-

--

-

REACTOR STATUS -_ 10001,,lF ;ON; OFF ION; OFF !ON; OFF ION; CFF OFF

I t - r I 1'

200

100

0 -

DASHED CURVE REPRESENTS CONTINUOUS 0 P E RATION

I AXIAL POSITION, z = 0.084 FT

900,

-

-

-

-

I

L 0.2 0.4 0.6 1.0 1.2

A 1.4 1 1.6 1.8

TIME, t - SECONDS

H910461-38

; 0.05 41 I fL -l 9 k 0.04 F v) er w I- z 5 0.03

FIG. 42

ON; OFF ION! OFF !ON; OFF ; O N ; OFF r-- -

-

-

-

TRANSIENT PROFILE OF MOLE-FRACTION OF HYDRAZINE FOR A HIGH THRUST ENGINE

I


STEADY-STATE MASS FLOW R A T E = 40.3 LB/FT’ - SEC

CATALYST BED CONFIGURATION: ALL 25-30 MESH PARTICLES


I1 - - - - - - - --- - - I I I I

DASHED CURVES REPRESENT CONTINUOUS OPERATION

I AXIAL POSITION, z = 0.084 FT 1

H9 1046 1-38 FIG. 43

0.8

0.7 W

I p. -I

2

5 0.6 E 5; K W I- ' 0.5

TRANSIENT PROFILE OF MOLE-FRACTION OF AMMONIA FOR A HIGH THRUST ENGINE

-

-

-

--

-

-

-


STEADY-STATE MASS FLOWRATE = 40.3 L B / F T ~ - SEC CATALYST B E D CONFIGURATION: A L L 25-30 MESH PARTICLES


0 z 3 0.4 LL 0 Z

I- 2

2 0.3 L W

0 z 0.2

0.1

_- .__I..._ . . __ REACTOR STATUS

OFF \ON: OFF ION( OFF ; O N \ OFF (04 OFF tONi OFF

-

-

-

-

-

-

-

-

0-


E G S I T I O N , z : ; . G I

0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8

TIME, t - SECONDS

H9 1046 1 -38 FIG. 44

TRANSIENT PROFILE OF MOLE-FRACTION OF NITROGEN FOR A HIGH THRUST ENGINE


S T E A D Y - S T A T E MASS FLOW = 40.3 L B / F T ~ - SEC

C A T A L Y S T BED CONFIGURATION : A L L 25-30 MESH PARTICLES


REACTOR STATUS _- OFF ; O N ; O F F

;ON[ OFF (ON! O F F ION' I I OFF O F F I .

OS5 ON1' W v)

DASHED CURVE REPRESENTS I AXIAL POSITION, CONTINUOUS OPERATION 1 z = 0.084 F T

7--

H9 10461 -38 FIG. 45 TRANSIENT PROFILE OF MOLE-FRACTION OF' HYDROGEN FOR A HIGH THRUST ENGINE



CATALYST B E D CONFIGURATION: A L L 25-30 MESH PARTICLES


1 .o

0.9

0.8

u: v)

I a 5 0.7

1 c I- v) oi

- 0.6

f z Z W 0

0.5 n > I U 0

0.4 2 I- U 4 K U I

w 0.3 -I 0 zz

0.2

0.1

0

REACTOR STATUS

IN : OFF :ON/ OFF OFF !ON! OFF ION; OFF /ON; O F F

I - - -

I DASHED CURVE REPRESENTS 1 CONTINUOUS OPERATION

! AXIAL POSITION, z = 0.084 F T I

0 0.2 0.4 0.6 0.8 1 .o 1.2 1.4 1.6 1.8 TIME, t - SECONDS

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