Simulation of Manufacturing Process of Nitrobenzene

8/15/2019 Simulation of Manufacturing Process of Nitrobenzene

1/83

DESIGN & SIMULATION OF NITROBENZENE MANUFACTURING PROCESS

FAMT ,Ratnagiri Page 1

INDEX

SR.NO. CONTENTS PAGE NO.

1 Chapter 1

Introduction

4

2 Chapter 2

Literature Review2.1. Process For Production Of Nitrobenzene2.2. Selection Of Process2.3. Manufacturing Process Of Nitrobenzene2.4. Chemical And Physical Properties

6

3 Chapter 3Thermodynamic Feasibility

3.1. Reaction Data For Formation Nitrobenzene3.2. Calculations

15

4 Chapter 4

Design Of Distillation Column

23

5 Chapter 5

Simulation Using Aspen

5.1 Introduction to Aspen5.2 Starting With Process Simulation

29

6 Chapter 6

Result summary6.1 Material Balance Over Reactor6.2 Material Balance Over Decanter6.3 Material Balance Over Distillation Column6.4 Overall Material Balance

49

7 Chapter 7

Conclusion

53

8 Chapter 8

References

55

9 APPENDIX A 58


2/83



FIGURE INDEX

FIGURE

NO.

FIGURE NAME PAGE NO.

1 2.1 Manufacturing Process Of Nitrobenzene 11

2 4.1 Rectification section 27

3 4.2 Stripping Section 28

4 5.1 Flowsheeting 34

5 5.2 Title Page 35

6 5.3 Component Entry 36

7 5.4 Selection Of Property Method 37

8 5.5 Mixer 38

9 5.6 Reactor 39

10 5.7 Reaction Input 40

11 5.8 Decanter 41

12 5.9 Distillation 42

13 5.10 Result Summary 43

14 5.11 Strem Result Over Mixer 44

15 5.12 Strem Result Over Reactor 45

16 5.13 Strem Result Over Decanter 46

17 5.14 Strem Result Over Distilation Column 47


3/83



TABLE INDEX

TABLE NO. TABLE NAME PAGE NO

1 2.1 Properties Of Benzene 11

2 2.2 Propetries Of Suphuric Acid 12

3 2.3 Properties Of Nitric Acid 13

4 2.4 Properties Of Nitrobenzene 14

5 2.5 Enthalpy Data At Standard State 16

6 2.5 Entropy Data At Standard State 16

7 2.5 Specific Heat Data At Standard State 17

8 5.1 Stream Result Overall 48

9 6.1 Material Balance Over Reactor 50

10 6.2 Material Balance Over Decanter 50

11 6.3 Material Balance Over Distillation Column 51

12 6.4 Overall Material Balance 52


4/83



CHAPTER-I

INTRODUCTION


5/83



INTRODUCTION

Nitrobenzene (some time called the oil of Mira-bane) C 6H5 NO 2 is pale yellow liquid

with an odour that resembles bitter almonds, Depending upon the compounds purity. Its

colour various from pale yellow to yellowish brown liquid boiling at 483 K (101 KPa) and

freezing at 287.7 K as bright yellow crystals. It is quite toxic to human system.

Nitrobenzene was first synthesized in 1834 by treating benzene with fuming nitric

acid. And it was first produced commercially in England in 1856. The elective‟s ease of

aromatic nitration has contributed significantly to the large and varied industrial application

of nitrobenzene, other aromatic nitro- compounds and their derivatives

A continues process for the production for the production has been developed byM/S.Biazzi of Switzerland. The advantages of this process are lower concentration of mixed

said used and higher reaction rate. The reactants are kept mixed under high speed agitation

(600 rpm) and cooling due to control feed rate and rapid agitation. The reaction time is about

15 – 20 minutes, where the yield is higher than 99% of theoretical .[4][5]


6/83



CHAPTER-II

LITERATURE REVIEW

2.1. Process For Production Of Nitrobenzene2.2. Selection Of Process2.3. Manufacturing Process Of Nitrobenzene2.4. Chemical And Physical Properties


7/83



LITERATURE REVIEW

2.1 PROCESS FOR PRODUCTION OF NITROBENZENE

Nitrobenzene is manufactured by nitration of benzene using mixture of Nitric and sulphuric

acid.

Nitration can be done by two processes. Via.

[1] Batch Process.

[2] Continuous process.

2.1.1 BATCH PROCESS

In batch process the nitrator is charged with benzene and mixed acid (HNO 3 32 – 39

%, H 2SO 4 60 -53 %, H 2O 8%) is added slowly below surface of benzene. The rate of

agitation is such that both the acid & benzene phases are in intimate contact. The feed rate of

mixed acid and the rate of cooling are such that during the entire period of acid addition, the

temperature of nitrator is maintained at 323 -328 K. after complete addition of acid, The acidand organic layers are drained into separate vessel from where spent acid is drawn off for

reconcentration. This crude product is washed with water to remove contamination in the

nitrobenzene and the aqueous sodium carbonate solution to remove small traces of nitro

phenols formed during nitration. Particularly when the product is to be further nitrated,

removal of nitrophenolic impurities is important, since they way undergo unwanted side

reaction during subsequent nitration. The product is further purified by distillation and the

yield is 95 – 98% of the theoretical.[4][5]


8/83



2.1.2 CONTINUOUS PROCESS

A continuous process for the production of nitrobenzene has been developed by M /

S.Biazzi of Switzerland. The advantages of this process are the lower concentration of mixed

acid is used and higher reaction, rates though the sequence of operations is the same as in bath process. Continuous nitrator with capacity of 150 lit. Can produce as a 7500 capacity

batch nitrator, but at the same time of quantity a reactants in nitrator is considerably small,

unlike the batch process.

Mixed acid and benzene are fed to nitrator in such that all nitric acid is utilized for nitraton of

benzene. The reactants are kept mixed under high speed agitation (600 rpm) and cooling.

Due to the controlled feed rate and rapid agitation, the reaction time is 15 to 20 minutes only

at reaction mixture is drawn off side of nitrator. The mixture is sent to decanter, where the, product is separated from spend acid for further processing. [4][5]

2.2 SELECTION OF PROCESS

Continuous process, in general, will be found to have the following to have the

following advantages over batch process.

[1] Lower Capital Cost.

[2] Safety

[3] Labour Usage.

2.2.1 LOWER CAPITAL COST

For a given rate of production, the equipment needed for a continuous process is

smaller than for a batch process. This is usually the striking different between the two types

of process. The reason for that is obvious since, it is not necessary to accumulate material in

a continuous process anywhere; the vessel is designed with capacity dictated by the rate of

reaction process step which they must accommodate. Alternatively, because of relatively


9/83



small size of continuous process equipment, it is often possible and excessively high in cost

for batch scale equipment. Thus for example Corrosion resistance alloys such as appropriate

S.S. may be detected for a batch plant because of cost. In case of S.S. corrosion problems are

completely eliminated.

2.2.2 SAFETY

Because of relatively small size of continuous process equipment, there is less

material in process at any time than at certain in a comparable batch process. At the

completion of batch process nitration and during its normal separation of product from spent

nitrating acid, the entire batch of an often hazardous compound will be present in the

equipment.

In the continuous process, only as much material need be present in hazardous

conditions as needed to again sufficient reaction of process time. In case of high explosive

made by nitration, this process has inherent safety factor is very attractive [3].

2.2.3 LABOUR USAGE

In the nitration filed the continuous process is usually more efficient labour usage

than a batch process. This is particularly true for small or medium scale production and for

hazardous products, since continuous processing minimizes the amount the material in

process on average. It is often possible to handle operations at one place that efficiency tends

to disappear as the scale of operations increases.

2.3 MANUFACTURING PROCESS OF NITROBENZENE

Nitrobenzene is manufactured commercially by direct nitration of benzene using a

mixture of nitric acid and sulphuric acid, which is commonly referred to as mixed acid for

nitrating acid. The reaction is conducted is specially build cast iron are S.S. reaction vessel


10/83



provided with agitator, external jacket and internal coils. Since two phases ate formed in

reaction mixture and reactant ate distributed between them. Rate of nitration is controlled by

transfer between the phases as well as by chemical kinetics.

Benzene used is of commercial quality. Mixed acid contain of 56 – 60 wt % H2SO

4, 20 – 26

wt% nitric acid and 15 – 18% water. Sulphuric acid used is of 94% - 98% concentration and

nitric acid commercial grade of 55% - 60% concentration.

Benzene is charged to the nitrator. Mixed acid is slowly added on surface of benzene from

dosing tank with stirring. The ratio of mixed acid to benzene is kept around 2.5 : 1.0. The

temperature mass is maintain initially at 25 – 30°C. So by high speed agitator and proper

cooling coils reaction temperature can maintained upto 50 – 55°C. By obvious agitation, the

interfacial area, of the reaction mixture is maintained as high as possible, thereby enhancingthe mass transfer of reactants and cooling coils, which control the temperature of highly

exothermic reaction .[4]

A slight excess of benzene usually is fed into the nitrator of ensure that the nitric acid in

mixed acid is formation of denitrobenzene. Reaction time is only 15 – 20 minutes because of

rapid and efficient agitation.

Nitrobenzene and spent acid are removed from the side reactor and send to decanter unit.

Organic and aqueous layers are formed, where two layers are separate in 10 to 20 minutes.

The aqueous phase or spent acid is drawn from the bottom and is concentrated in a sulphuric

acid is drawn from the bottom and is concentrated in a sulphuric acid reconcentration step or

is recycled to the nitrator, where it is mixed nitric acid and sulphuric acid immediately prior

to being fed into nitrator.

The crude Nitrobenzene can used directly for production of aniline if required, otherwise the

crude nitrobenzene flows through a series of washer – separators, where residual acid is

removed by washing with a dilute sodium carbonate solution followed by final washing with

water.The product is then distilled to remove benzene and the nitrobenzene can be refined by

vacuum distillation. Theoretical yields are 96 – 99 %. The nitration process is unavoidably

associated with the disposal of waste water from washing step. This water principally

contains Nitrobenzene, some sodium carbonate and inorganic salts from the neutralized spent


11/83



acid which was present in the product. Generally, the waste water is extracted with benzene

to remove the nitrobenzene and the benzene that is dissolved in the water is stripped from

water prior to the final waste treatment. [6]

Fig No-2.1 Manufacturing Process Of Nitrobenzene

2.4 CHEMICAL AND PHYSICAL PROPETRIES [7]

2.4.1 PROPERTIES OF BENZENE

PHYSICAL PROPERTY-

PROPERTY VALUE

Molecular Weight 78.11

Melting Point, °C 5-533

Boiling Point, °C 80.1

Density, Kg/cum 873.7


12/83



Refractive index 1.49792

Viscosity (absolute, at 20°C) 0.6468

Flash point, °C -11.1

Heat of fusion, kJ/kmole 9.847

Table No-2.1 Properties Of Benzene

CHEMICAL PROPERTY [14][15][16]

REACTION WITH WATER:-

Water and benzene are non-react ive unless high and pressure are applied .

2.4.2 PROPETRIES OF SUPHURIC ACID

PHYSICAL PROPERTY-

PROPERTY VALUE


Boiling Point, °c 330.0

Density, at 20°C, gm/cc 1.834

Flash Point None

Vapour pressure at 145°C mmHg 1.0

TLV, mg/cum. 1.0

Freezing Point, °C 10.48

Table No-2.2 Propetries Of Suphuric Acid


13/83



CHEMICAL PROPERTY [14][15][16]

REACTION WITH WATER:-

Has great affinity for water, absorbs atmospheric moisture and absorbs water from organic

material causing charring. Sulphuric Acid reacts with water vigorously liberating large

amount of heat.

REACTION WITH METAL AND OTHER ELEMENTS:-

When cold, it reacts with metal including platinum when not, reactivity is intensified.

Sulphuric acid on reaction with metals causes liberations of flammable hydrogen.

Cu + H 2SO 4 → CuSO 4 + H 2

Zn + H 2SO 4 → ZnSO 4 + H 2

2.4.3 PROPERTIES OF NITRIC ACID

PHYSICAL PROPERTY-

PROPERTY VALUE


Boiling Point 86.0

Melting point °C -42.0

Density, at 20°C,gm/cc 1.502

Flash point None

Solubility in water Soluble in water

TLV, mg/cum. 2-5

Freezing point, °C 10.48

Table No. 2.3 Properties Of Nitric Acid


14/83



CHEMICAL PROPERTIES :-

REACTION WITH WATER :-

Nitric Acid reacts with water to produce heat, toxic and corrosive fumes.

REACTION WITH METALS AND OTHER ELEMENTS :-

Nitric acid is corrosive to most of metals like zinc to form nitrate with evolution of hydrogen.

Cu + 2HNO 3 → Cu (NO 3)2 + H 2

Zn + 2HNO 3 → Zn (NO 3)2 + H 2

2.4.4 PROPERTIES OF NITROBENZENE

PHYSICAL PROPERTY-

PROPERTY VALUE


Boiling Point, °C 201.9

Melting point, °C 5.85

Density, at 20°C, gm/cc 1.344

Flash point 88.0

Auto ignition temp., °C 482.0

Explosive limit (at 93°) 1.8 Vol % in air

Vapour density 4.1

Table No. 2.4 Properties Of Nitrobenzene


15/83



CHAPTER III

THERMODYNAMIC FEASIBILITY

3.1. Reaction Data For Formation Nitrobenzene

3.2. Calculations


16/83



THERMODYNAMIC FEASIBILITY

3.1 REACTION DATA FOR FORMATION NITROBENZENE [7]

REACTION:-

C6H6 + HNO 3 C 6 H5 NO 2 + H 2O

DATA :-

HEAT OF FORMATION ( kcal/gmole)

Benzene (liquid) 11.71

Nitrobenzen (liquid) 13.76

Nitric acid (liquid) -41-61

Water (liquid) -68.315

Table No. 2.5 Enthalpy Data At Standard State

ENTHROPY kJ/(kmol.K)


Nitrobenzene (Liquid) 364.61

Nitric acid (liquid) 110.113

Water (liquid) 69.92

Table No. 2.6 Entropy Data At Standard State


17/83



SPECIFIC HEAT AT 25 °C kJ/(kmol.K)


Nitrobenzene (liquid) 185.361

Nitric acid (liquid) 111.113

Water (liquid) 75.362

Table No. 2.7 Specific Heat Data At Standard State

3.2 CALCULATIONS [11]

From heat of formation data:

∆HR = H PRODUCTS - H REACTANTS

= ( H NB + H WATER ) - ( H BENZENE + H NITRIC ACID )

= ( 13.76 – 68.315 ) - (11.71 – 41.61)

∆HR = -24.655 kcal/gmmole

∆HR = -103157 kJ/(kmol)

From specific heat data:

Cpavg = Cp PRODUCT - Cp REACTANT

= ( Cp NB + Cp WATER ) - ( Cp BENZENE + Cp NITRIC ACID )


18/83



= ( 185.361 + 75.362 ) - ( 91.73 + 111.113 )

Cpavg = 57.88 kJ/(kmol.K)

From entropy data:

∆S = S PRODUCTS - S REACTANTS

= ( S NB + S WATER ) - ( S BENZENE + S NITRIC ACID )

= ( 364.61 + 69.92 ) - ( 172.91 + 110.113 )

∆S = 151.507 kJ/(kmol.K)

For ∆H R At Reaction Temperature:

∆HR = ∆H° - Cp.T

∆H° = ∆H R + Cp.T

= -103157 + 57.88 × 298

= -85908.76 kJ/(kmol)

Therefore, ∆H R at 323 K,

∆HR = -85908.76 – ( 57.88 ×323 )

= -104604 kJ/(kmol)

Similarly, for ∆S At Reaction Temperature:

∆S = ∆S° + CplnT


19/83



∆S°= ∆S - CplnT

= 157.507 - 57.88 ×In (298)

= -178.24 kJ/(kmol.K)

Therefore, ∆S at 323 K,

∆S = -178.507 + 57.88 ×In (323)

= 156.17 kJ/(kmol.K)

Now using Standard free energy change relation,

∆G° = ∆H R - T∆S

= -104604 – (323×156.17)

= -155046.91 kJ/(kmol)

Since ∆G° is negative it can thermodynamically feasible Reaction

By using Van‟t Hoff Isotherm,

∆G° = -RT lnKp

lnKp =

=

= 57.73

Kp = 1.18 ×1025

Since Kp = Kx×P ∆n

For our reaction,

∆n = (1+1)-(1-1)


20/83



= 0

Kp = ×P 0

Kp = = Kx

Now,taking material balance,

Composition of mixed acid(Weight basis):

25% Nitric acid

58% Sulphuric acid

17% Water

Consider 1000 kg of mixed acid.

Nitric acid 250 kg = 3.97 kmole

Water 170kg = 9.44 kmole

Sulphuric acid 580 kg = 5.92 kmole

----------------------------

Total moles 19.33 kmole


21/83



Mole % of Nitric acid = 20.5 %

Water = 48.8 %

Sulphuric acid = 30.7 %

But benzene mixed acid

1----------------------------> 2.5

400kg 19.314

Moles of benzene = 1 ----------------> 3.766 moles of

Moles of acid = 3.766 X 0.205 = 0.772 moles

Reaction of nitrobenzene

C6H6 + HNO 3 → C6 H5 NO 2 + H 2O


22/83



Initially 1 0.772 0 0

Reacted X X X X

At. equilibrium (1-X) (0.772-X) X X

Kx = X 2

-----------------------

(1 - X) (0.772 - X)

X2

1.18 ×10 25 = ---------------------------------------

X2 - 1.73 X + 0.73

X2 - 1.772 X + 0.772 = 0

X = 0.772

Extent of reaction = 0.772


23/83



CHAPTER IV

DESIGN OF DISTILLATION COLUMN


24/83



DESIGN OF DISTILLATION COLUMN [10]

Basis ; 1 hour of operation.

Mass flow rate of feed = 740.75 kg/hr.

Mass flow rate of distillate = 32.3 kg/hr.

Mass flow rate of bottom = 708.38 kg/hr.

Xf =

= 0.317/1.401

= 0.226

Xd = 2.8075/3.048

= 0.92

Xw = 0.0036/1.08667

= 0.003

Average Molecular weight of feed = 110.556

Feed rate = 593.568 kg/hr

Slope of q-line ;

We know that q = Hg-Hf / Hg-Hl

q=1

slope of q-line:

slope of q-line = q/q-1

= 1/1-1

Tan- 1(α) = 0


25/83



q line is st.line

Xd / Rm+1 = 0.05

Rm+1 = 1/0.05

Rm+1 = 20

Rm = 19

R = 1.2 Rm

R = 22.8 ∼ 23

Xd = 1 = 0.042

Rm+1= 23+1 =24

From Mc-cabe Thile Graph

X 0 0.01 0.02 0.03 0.045 0.07 0.10 0.155 0.20 0.30

Y 0 0.03 0.485 0.63 0.74 0.82 0.88 0.92 0.94 0.964

Ideal Plate = 16 (From Graph)

Actual Plate = Ideal/n = 16/0.6

Actual Plate = 26.66

Height:

Plate Spacing = 450 mm = 0.45m

Ht = (Actual Plate-1)×0.45 + 2(0.45)

= 12.45m


26/83



Diameter :

Vap rate = v = D(R+1)

= 0.0087(23+1)

n = 0.21 kmole/hr

Top Column :

Vol.rate = nRT/P

= 0.21×8.314×103×(82+273)/ 1.01325×105 = 6.1170 m 3/hr

Vol rate = 1.7×10 -3 m3/sec

Velocity = 1 m/sec

Area = Vol rate / Velocity

= 1.7×10 -3 /1 = 1.7×10 -3 m2

Area = π D 2 /4

D2 = 4A /π

D = 0.047 m

Bottom column:

Vol.rate = nRT/P

= 0.21×8.314×103×(210+273)/ 1.01325×105 = 8.32 m 3/hr

Area = Vol .rate / Velocity

Velocity = 1 m/sec

Area = 2.31×10 -3 m2

A = π D 2 / 4


27/83



D2 = 4A /π

D = 0.054 m

Both diameters are approximately same ,

we choose the larger diameter (i.e) bottom diameter

Bottom diameter D= 0.054 m

DESIGN SUMMARY

Ideal plate = 16.00

Actual Plates = 26.66

Column Height = 12.45 m

Column Diameter = 0.054 m

Fig No. 4.1 Rectification Section


28/83



Fig No-4.2 Stripping Section


29/83



CHAPTER V

SIMULATION USING ASPEN


30/83



SIMULATION USING ASPEN

5.1 INTRODUCTION TO ASPEN [8]

5.1.1 What is a Process Flowsheet?

Process flowsheet can simply be defined as a blue print of a plant or part of it. It

identifies all feed streams, unit operations, streams that inter-connect the unit Operations and

finally the product streams. Operating conditions and other technical Details are included

depending on the detail level of the flowsheet. The level can vary from a rough sketch to a

very detailed design specification of a complex plant. For steady-state operation, any process

flowsheet leads to a finite set of algebraic equations. For a case where we have only one

reactor with appropriate feed and Product streams the number of equations may be

manageable by manual hand calculations or simple computer applications. However, as the

complexity of a flowsheet Increases and when distillation columns, heat exchangers,

absorbers with many purge and recycle streams come into the picture the number of

equations easily approach many ten thousands. In these cases, solving the set of algebraic

equations becomes a Challenge in it. However, there are computer applications called process flowsheet simulators specialized in solving these kinds of large equation sets. Some

well-known process flowsheet simulators are Aspen Plus, ChemCad and PRO/II.These

products have highly refined user interfaces and on-line component databases. They are used

in real world applications from interpreting laboratory scale data to monitoring a full scale

plant.

5.1.2 Advantages of using a process flowsheet simulator

The use of a process flowsheet simulator is beneficial in all the three stages of aPlant:

research & development, design and production. In research & development they help to cut

down on laboratory experiments and pilot plant runs. In design stage they enable a speedier

development with simpler comparisons of various alternatives.


31/83



Finally, in the production stage they can be used for risk-free analysis of various what-if

scenarios

5.1.3 Disadvantages of using a process flowsheet simulator

Disadvantages of using a process flowsheet simulatorManual solution of a problem

usually forces someone to think deeper on theProblem, find novel approaches to solve it, and

evaluate and re-evaluate the Assumptions closer. A drawback of process flowsheet

simulators may be cited as the Lack of this detailed interaction with the problem. This might

act as a double edged Sword. On one side it hides the complexities of a problem so you can

concentrate on the real issues at hand. On the other side this hiding may also hide some

important Understanding of the problem as well, [8]

5.1.4 History

In 1970s the researchers at MIT‟s Energy Laboratory developed a prototype

forProcess simulation. They called it Advanced System for Process Engineering

(ASPEN).This software has been commercialized in 1980‟s by the foundation of a

companyNamed AspenTech. AspenTech is now a publicly traded company that employs

1800People worldwide and offers a complete integrated solution to chemical

processIndustries.This sophisticated software package can be used in almost every aspect of

processengineering from design stage to cost and profitability analysis. It has a built-in

modelLibrary for distillation columns, separators, heat exchangers, reactors, etc. Custom

orPropriety models can extend its model library. These user models are created with

FORTRAN subroutines or Excel worksheets and added to its model library. Using

VisualBasic to add input forms for the user models makes them indistinguishable from

theBuilt-in ones. It has a built-in property databank for thermodynamic and physicalParameters. During the calculation of the flow sheet any missing parameter can

beestimated automatically by various group contribution methods.In this workshop we will

only scratch the surface of this tool. We will discuss itsAdvantages and disadvantages. Our

focus will be on reactors and our goal is to provideyou with a smooth and simple introduction


32/83



to Aspen Plus. Let‟s start our workshop bylearning how to access Aspen Plus at the

University of Michigan.

5.1.5 What is an Aspen plus Process Simulation Model?

A process consists of components being mixed, separated, heated, cooled a Converted

by unit operations. These components are transferred from unit to unitthrough process stream

you can translate a process into an Aspen plus process simulation model bydoing the

following steps:

1. Define the process flowsheet configuration. To do this step, you:

Define the unit operations in the process

Define the process streams that flow between these unit operations

Select unit operation models from the Aspen Plus model library to

Describe each unit operation

2. Specify the chemical components in the process. You can take these

Components from the Aspen Plus databanks, or you can define them.

3. Choose appropriate thermodynamic models from those available in Aspen

Plus, to represent the physical properties of the components and mixtures in

The process.

4. Specify the component flow rates and the thermodynamic conditions (for

Example, temperature and pressure) of feed streams to the process.

5. Specify the operating conditions for the unit operations in the flowsheet.

When you have specified this information, you have defined an Aspen Plus

Process simulation model of your process. You can use the Aspen plus processSimulation

model to predict process behaviour.


33/83



With Aspen Plus you can interactively change specifications, such as

flowsheetConfiguration, operating conditions, and feed compositions, to run new cases

andAnalyse alternatives. In addition to process simulation, Aspen Plus allows you to perform

a wide rangeof other tasks such as estimating and regressing physical properties,

generatingCustom graphical and tabular output results, data-fitting plant data toSimulationmodels, costing your plant, optimizing your process, and interfacingResults to spread sheets.

5.1.6 Why Use Process Simulation?

Process simulation allows you to predict the behaviour of approves by using basicEngineering relationships, such as mass and energy balances, and phase and Chemical

equilibrium. Given reliable thermodynamic data, realistic operating Conditions, and rigorous

equipment models, you can simulate actual plant Behaviours. Process simulation enables you

to run many cases conduct "what if" Analyses, and perform sensitivity studies and

optimization runs. With simulation, you can design better plant and increase profitability in

existing plants.


34/83



5.2 STARTING WITH PROCESS SIMULATION

1] First stating with Blank Simulation we must design our required flowsheet with proper

stream names & block names .each stream is properly connect to the proper unit.After doing

this we click Next to the required input step by step.

Fig No 5.1-Flowsheeting


35/83



2] we input Title of our simulation with all units are in SI units.

Fig No 5.2-Title Page


36/83



3] We input our components that takes part in process operation,all conventional types

It involves nitrobenzene,benzene,water,sulphuric acid,nitric acid.

Fig No 5.3 – Component Entry


37/83



4] This is the step where you put property method.From our investigation in aspen running

plant we know that NRTL is the best property method applied where large water usage inoperation or process.

Fig No 5.4- Selection Of Property Method


38/83



5] Then we come at Block of Mixer where we fed H 2SO 4, H 2O, HNO 3 in desired proportion

to make Mixed acid.In mixer we operate at normal temperature & pressure.

Fig No 5.5-Mixer


39/83



6] Next to we selected stoichiometric reactor since we know only the extent of reaction &

stoichiometric reaction coefficients operating at 50 °C

Fig No 5.6-Reactor


40/83



7] Insert our reaction in new option with correct coefficient

Fig No 5.7 Reaction Input


41/83



8] Moving on to decanter we fed extra water to this unit in order to remove sulphuric acid

effectively.we select nitrobenzene is our key component

Fig No 5.8-Decanter


42/83



9] Distillation column is where we obtained our desired product in Bottom stream from data

we find out optimum feed ratio

Fig No 5.9- Distilation


43/83



10] Final next to Run the simulation

Summary obtained,

Fig No 5.10-Result Summary


44/83



11 Now we take stream result over each block

First is Mixer which has 3 inlet stream & 1 outlet stream

Fig No 5.11-Strem Result Over Mixer


45/83



12] Second block is stoichiometric reactor where we provide benzene with mixed acid in

1:2.5 proportion.Crude nitrobenzene is obtained .

Fig No 5.12-Strem Result Over Reactor


46/83



13] Third stream result over Decanter

Fig No 5.13 -Strem Result Over Decanter


47/83



14] Last stream result over a distillation column in the bottom stream we get our final

product

Fig No 5.14 -Strem Result Over Distilation Column


48/83



15] Steam result obtained from overall result

Table No 5.1-Strem Result Overall


49/83



CHAPTERVI

RESULT SUMMARY


50/83



RESULT SUMMARY

6.1 MATERIAL BALANCE OVER REACTOR

SR. NO COMPONENTS INPUT(kg/hr) OUTPUT(kg/hr)

1 BENZENE 400 91.07

2 NITROBENZENE - 486.2

3 WATER1000

241.84

4 NITRIC ACID 0.89

5 SULPHURIC ACID 580

TOTAL 1400 1400

Table No.6.1 Material Balance Over Reactor

6.2 MATERIAL BALANCE OVER DEACNTER

Table No.6.2 Material Balance Over Decanter

INPUT(kg/hr)

OUTPUT(kg/hr)

SR. NO

COMPONENTS SPENT ACIDSTREAM

ORGANIC PHASE

1 BENZENE 91.07 2.09 88.982 NITROBENZENE 486.2 9.88 476.32

3 WATER 241.84+2000 2241.43 0.41

4 NITRIC ACID 0.89 0.89 -

5 SULPHURICACID

580 553.51 26.49

TOTAL 3400 3400


51/83



6.3 MATERIAL BALANCE OVER DISTILLATION COLUMN

INPUT(kg/hr)

OUTPUT(kg/hr)

SR. NO

COMPONENTS TOP PRODUCT BOTTOM PRODUCT

1 BENZENE 88.98 78.6 10.38

2 NITROBENZENE 476.32 - 476.32

3 WATER 0.41 0.41 -

4 NITRIC ACID - - -

5 SULPHURIC ACID 26.49 - 26.49

TOTAL 592.2 592.2

Table No.6.3 Material Balance Over Distillation Column


52/83



6.4 OVERALL MATERIAL BALANCE

Table No. 6.4 Overall Material Balance

Conversion of benzene is 77 %

Purity of Nitrobenzene in bottom product is 92.8 %.

INPUT(kg/hr)

OUTPUT(kg/hr)

SR.

NO

COMPONENTS TOTAL SPENT

ACID

STREAM

TOP PDT

STREAM

BOTTOM

PDT

STREAM

1 BENZENE 400 2.09 78.6 10.38

2 NITRIC ACID 250 0.89 - -

3 SULPHURIC

ACID

580 553.51 - 26.49

4 WATER 170 + 2000 2241.43 0.41 -

5 NITROBENZENE - 9.88 - 476.32

TOTAL(kg/hr) 3400 3400


53/83



CHAPTER VII

CONCLUSION


54/83



CONCLUSION

It is very important for any process to kow that parameters like composition, streams,temperature, pressure etc may affect the production rate.One must have perform pilot plant in

order to know this, so each time we need manual calculation to get desired results,this is so

time consuming. So the use of simulaters like ASPEN, CHEMCAD are helpful.Simulation &

modeling useful in doing risk analysis in production process.

In our project we simulate continuous process for nitrobenzene production using

benzene nitration.In that we know about how actually parameters mention above may affect

each stream.For example we first added calculated amount of extra water to decanter,butfrom that action we know that how much extent it affect the each stream,so we are finaly able

to find the optimum amount of water required for operation.

Generally it is difficult to obtain desired result manually that is why we simulate it

using ASPEN PLUS .And we searching new techniques as possible in order to get the

optimum production. Also we can check where is the opportunity to increase the conversion

& reduce the losses as well as maintenance cost.


55/83



CHAPTER VIII

REFERENCES


56/83



REFERENCES

Books,

[1]B.I. Bhatt & S.M. Vora. “ Stoichiometry ”, Tata – Mcgraw Hill Publishing Co. Ltd.

[2]Dryden C. E., “Drydens Outline Of Chemical Technology ”. East – West Press Pvt.

Ltd;(536)

[3]G. D. Muir, “Hazardous In Chemical Laboratory ” The Chemical Society, London.

[4]Kirk – Othmer „Encyclopedia Of Chemical Technology‟.Vol. – 15. Wiley

Intenscience Publications, 1979.(138-139)

[5]P.H.Groggins .„Unit Process In Porganic Synthesis.‟ Mcgraw – Hill InternationalBook Co.

[6]R.Norris Shreve & Joseph A. Brink Jr.„Chemical Process Industries‟.Mcgraw – Hill

International Publications.(776-778)

[7]Robert H. Perry „Perry‟s Chemical Engineering Handbook‟.Mcgraw – Hill

International Publications.(642-644)

[8]Amiya K. Jana. „ Process Simulation And Controle Using Aspen‟.PHI Learning Private

Limited ,Second Edition ,2012

[9]Bhattacharya A., Purohit V. C., Suarez, V.; Tichkule, R; Parmer, G.; Rinaldi, F.

(2006). "One-step reductive amidation of nitro arenes: application in the synthesis of

Acetaminophen" Volume 47, Issue 11, 13 March 2006, Pages (1861 – 1864)

[10]M.V.Joshi,Mahajani, Joshi's Process Equipment Design, Macmillan, 2009

[11] K.A.Gavane,” Chemical Reaction Engineering- I”,Nirali Publication,2012, Chapter 6

(6.1-6.15)

Journal Papers,

[12] R. D. BIGGS and R. R. WHITE „ Rate of Nitration of Benzene with Mixed Acid‟

University of Michigan, Ann Arbor, Michigan 2000

[13]J. Chil. Chem. Soc. vol.57 no.2 Concepción 2012, págs: 1194-1198.


57/83



[14]V. Dubois, G. James, J.L. Dallons, A. Van Geysel, In Catalysis of Organic Reactions,

M. Ford, Ed; Marcel Dekker, New York, 1994, Vol.82, p. 1.

[15] Laali, Kenneth K., and Volkar J. Gettwert. “Electrophilic Nitration of Aromatics in

Ionic Liquid Solvents.” The Journal of Organic Chemistry 66 (Dec. 2000): 35 -40.

American Chemical Society.[16]Sauls, Thomas W., Walter H. Rueggeberg, and Samuel L. Norwood. “On the

Mechanism of Sulfonation of the Aromatic Nucleus and Sulfone Formation.” The

Journal of Organic Chemistry 66 (1955): 455-465. American Chemical Society.


58/83



APPENDIX A


59/83



SIMULATION REPORT

ASPEN PLUS PLAT: WIN32 VER: 10.2.1 04/28/2014 PAGE 1

MANUFCTURING OF NITROBENZENE

RUN CONTROL SECTION

RUN CONTROL INFORMATION

-----------------------

THIS COPY OF ASPEN PLUS LICENSED TO

TYPE OF RUN: NEW

INPUT FILE NAME: _0812ogh.inm

OUTPUT PROBLEM DATA FILE NAME: _0335nde VERSION NO. 1

LOCATED IN:


60/83



PDF SIZE USED FOR INPUT TRANSLATION:

NUMBER OF FILE RECORDS (PSIZE) = 0

NUMBER OF IN-CORE RECORDS = 256

PSIZE NEEDED FOR SIMULATION = 1

CALLING PROGRAM NAME: apmain

LOCATED IN: C:\PROGRA~2\ASPENT~1\ASPENP~1.2\Engine\xeq

SIMULATION REQUESTED FOR ENTIRE FLOWSHEET



INPUT SECTION

INPUT FILE(S)

-------------

;

;Input Summary created by Aspen Plus Rel. 10.2.1 at 19:39:35 Sun Apr 27, 2014

;Directory G:\Aspen new\aspen save Filename _0812ogh.dan

;


61/83



TITLE 'MANUFCTURING OF NITROBENZENE'

IN-UNITS SI

DEF-STREAMS CONVEN ALL

SIM-OPTIONS

IN-UNITS ENG

SIM-OPTIONS NPHASE=1 PHASE=L ATM-PRES=101325.

DATABANKS PURE10 / AQUEOUS / SOLIDS / INORGANIC / &

NOASPENPCD

PROP-SOURCES PURE10 / AQUEOUS / SOLIDS / INORGANIC

COMPONENTS

C6H5NO2 C6H5NO2 /

H2SO4 H2SO4 /

H2O H2O /

HNO3 HNO3 /

C6H6 C6H6


62/83



FLOWSHEET NBMFG

BLOCK RSTO IN=C6H6 MIXACID OUT=CNB

BLOCK DECANTER IN=CNB OUT=SPA ORGANIC

BLOCK DIST IN=ORGANIC OUT=TOP BOTTOM

BLOCK MIXER IN=HNO3 H2O H2SO4 OUT=MIXACID

DEF-STREAMS CONVEN NBMFG

PROPERTIES NRTL

PROP-DATA NRTL-1

IN-UNITS SI

PROP-LIST NRTL

BPVAL C6H5NO2 H2O -5.154900000 2270.617200 .2000000000 0.0 &

0.0 0.0 273.1500000 379.7500000

BPVAL H2O C6H5NO2 5.854700000 229.4967000 .2000000000 0.0 &

0.0 0.0 273.1500000 379.7500000

BPVAL C6H5NO2 C6H6 -.8730000000 630.1689000 .3000000000 0.0 &

0.0 0.0 343.1500000 484.1500000

BPVAL C6H6 C6H5NO2 -1.289300000 98.83280000 .3000000000 0.0 &

0.0 0.0 343.1500000 484.1500000


63/83



BPVAL H2O C6H6 140.0874000 -5954.307100 .2000000000 0.0 &

-20.02540000 0.0 273.9500000 350.1500000

BPVAL C6H6 H2O 45.19050000 591.3676000 .2000000000 0.0 &



INPUT SECTION

INPUT FILE(S) (CONTINUED)

-7.562900000 0.0 273.9500000 350.1500000

STREAM C6H6

SUBSTREAM MIXED TEMP=298. PRES=101325. MASS-FLOW=400.

MASS-FRAC C6H6 1.

STREAM H2O


MASS-FRAC H2O 1.

STREAM H2SO4


64/83




MASS-FRAC H2SO4 0.98

STREAM HNO3


MASS-FRAC HNO3 0.6

BLOCK MIXER MIXER

PARAM PRES=101325. T-EST=298.

BLOCK DECANTER DECANTER

PARAM TEMP=298. PRES=101325. L2-COMPS=C6H5NO2

;

;Input file created by Aspen Plus Rel. 10.2.1 at 00:20:55 Mon Apr 28, 2014

;Directory G:\Aspen new\aspen save Runid simu1

;

BLOCK DIST DISTL

PARAM NSTAGE=26 FEED-LOC=16 RR=0.45 PTOP=101325. &


65/83



PBOT=101325. D:F=0.205

BLOCK RSTO RSTOIC

PARAM TEMP=323. PRES=101325.

STOIC 1 MIXED C6H6 -1. / HNO3 -1. / C6H5NO2 1. / H2O &

1.

CONV 1 MIXED C6H6 0.772

REPORT INPUT

;

;

;

;

;

;



;




66/83



INPUT SECTION

INPUT FILE(S) (CONTINUED)

STREAM EXH2O

SUBSTREAM MIXED TEMP=298. PRES=101325. MOLE-FLOW=0.0309

MOLE-FRAC H2O 1.

;


;Directory G:\Aspen new\aspen save Runid SIMU1

;

FLOWSHEET NBMFG


BLOCK DECANTER IN=CNB EXH2O OUT=SPA ORGANIC

BLOCK DIST IN=ORGANIC OUT=TOP BOTTOM


;




67/83



;

FLOWSHEET NBMFG


BLOCK DECANTER IN=CNB EXH2O OUT=SPA ORGANIC

BLOCK DIST IN=2 OUT=TOP BOTTOM


BLOCK B1 IN=ORGANIC OUT=2



FLOWSHEET SECTION

FLOWSHEET CONNECTIVITY BY STREAMS

---------------------------------

STREAM SOURCE DEST STREAM SOURCE DEST

EXH2O ---- DECANTER C6H6 ---- RSTO

H2SO4 ---- MIXER H2O ---- MIXER

HNO3 ---- MIXER CNB RSTO DECANTER

SPA DECANTER ---- ORGANIC DECANTER DIST


68/83



TOP DIST ---- BOTTOM DIST ----

MIXACID MIXER RSTO

FLOWSHEET CONNECTIVITY BY BLOCKS

--------------------------------

BLOCK INLETS OUTLETS

RSTO C6H6 MIXACID CNB

DECANTER CNB EXH2O SPA ORGANIC

DIST ORGANIC TOP BOTTOM

MIXER HNO3 H2O H2SO4 MIXACID

COMPUTATIONAL SEQUENCE

----------------------

SEQUENCE USED WAS:

MIXER RSTO DECANTER DIST

OVERALL FLOWSHEET BALANCE

-------------------------

*** MASS AND ENERGY BALANCE ***


69/83



IN OUT GENERATION RELATIVE DIFF.

CONVENTIONAL COMPONENTS

(KMOL/SEC)

C6H5NO2 0.000000E+00 0.109812E-02 0.109812E-02 -0.336175E-06

H2SO4 0.164266E-02 0.164266E-02 0.000000E+00 -0.189866E-08

H2O 0.335212E-01 0.346193E-01 0.109812E-02 0.138954E-07

HNO3 0.110207E-02 0.395223E-05 -0.109812E-02 -0.680900E-11

C6H6 0.142243E-02 0.324314E-03 -0.109812E-02 -0.764627E-07

TOTAL BALANCE

MOLE(KMOL/SEC) 0.376884E-01 0.376884E-01 0.000000E+00 0.000000E+00

MASS(KG/SEC ) 0.945561 0.945561 -0.482081E-07

ENTHALPY(WATT ) -0.110013E+08 -0.111195E+08 0.106313E-01



PHYSICAL PROPERTIES SECTION

COMPONENTS

----------

ID TYPE FORMULA NAME OR ALIAS REPORT NAME

C6H5NO2 C C6H5NO2 C6H5NO2 C6H5NO2

H2SO4 C H2SO4 H2SO4 H2SO4


70/83



H2O C H2O H2O H2O

HNO3 C HNO3 HNO3 HNO3

C6H6 C C6H6 C6H6 C6H6



U-O-S BLOCK SECTION

BLOCK: DECANTER MODEL: DECANTER

--------------------------------

INLET STREAMS: CNB EXH2O

FIRST LIQUID OUTLET: SPA

SECOND LIQUID OUTLET: ORGANIC

PROPERTY OPTION SET: NRTL RENON (NRTL) / IDEAL GAS


IN OUT RELATIVE DIFF.

TOTAL BALANCE

MOLE(KMOL/SEC) 0.376884E-01 0.376884E-01 0.000000E+00

MASS(KG/SEC ) 0.945561 0.945561 -0.482081E-07



71/83


72/83



L1-L2 PHASE EQUILIBRIUM :

COMP F X1 X2 K

C6H5NO2 0.029137 0.00061841 0.72129 1,166.36

H2SO4 0.043585 0.043344 0.049433 1.14047

H2O 0.91857 0.95573 0.016631 0.017401

HNO3 0.00010487 0.00010429 0.00011894 1.14047

C6H6 0.0086051 0.00020300 0.21253 1,046.96



U-O-S BLOCK SECTION

BLOCK: DIST MODEL: DISTL

-----------------------------

INLET STREAM: ORGANIC

CONDENSER OUTLET: TOP

REBOILER OUTLET: BOTTOM




TOTAL BALANCE


73/83



MOLE(KMOL/SEC) 0.149140E-02 0.149140E-02 0.000000E+00

MASS(KG/SEC ) 0.164883 0.164883 0.338098E-08

ENTHALPY(WATT ) -34983.6 8548.66 -1.24436

*** INPUT DATA ***

THEORETICAL STAGES 26

FEED STAGE NO. FROM TOP 16

REFLUX RATIO 0.45000

TOP STAGE PRESSURE (N/SQM ) 101,325.

BOTTOM STAGE PRESSURE (N/SQM ) 101,325.

DISTILLATE TO FEED RATIO 0.20500

CONDENSER TYPE: TOTAL CONDENSER

*** RESULTS ***

FEED-QUALITY -0.31849

FEED STAGE TEMPERATURE (K ) 365.058

TOP STAGE TEMPERATURE (K ) 324.418

BOTTOM STAGE TEMPERATURE (K ) 478.860

CONDENSER COOLING REQUIRED (WATT ) 14,284.2

NET CONDENSER DUTY (WATT ) -14,284.2

REBOILER HEATING REQUIRED (WATT ) 57,816.5

NET REBOILER DUTY (WATT ) 57,816.5


74/83



BLOCK: MIXER MODEL: MIXER

-----------------------------

INLET STREAMS: HNO3 H2O H2SO4

OUTLET STREAM: MIXACID




U-O-S BLOCK SECTION

BLOCK: MIXER MODEL: MIXER (CONTINUED)



TOTAL BALANCE

MOLE(KMOL/SEC) 0.536596E-02 0.536596E-02 0.000000E+00

MASS(KG/SEC ) 0.277778 0.277778 -0.199840E-15


*** INPUT DATA ***

ONE PHASE FLASH SPECIFIED PHASE IS LIQUID


75/83



MAXIMUM NO. ITERATIONS 30

CONVERGENCE TOLERANCE 0.00010000

OUTLET PRESSURE N/SQM 101,325.

BLOCK: RSTO MODEL: RSTOIC

------------------------------

INLET STREAMS: C6H6 MIXACID

OUTLET STREAM: CNB



IN OUT GENERATION RELATIVE DIFF.

TOTAL BALANCE

MOLE(KMOL/SEC) 0.678839E-02 0.678839E-02 0.000000E+00 0.000000E+00

MASS(KG/SEC ) 0.388889 0.388889 0.000000E+00


*** INPUT DATA ***

SIMULTANEOUS REACTIONS

STOICHIOMETRY MATRIX:


76/83



REACTION # 1:

SUBSTREAM MIXED :

C6H5NO2 1.00 H2O 1.00 HNO3 -1.00 C6H6 -1.00

REACTION CONVERSION SPECS: NUMBER= 1

REACTION # 1:

SUBSTREAM:MIXED KEY COMP:C6H6 CONV FRAC: 0.7720



U-O-S BLOCK SECTION

BLOCK: RSTO MODEL: RSTOIC (CONTINUED)

ONE PHASE TP FLASH SPECIFIED PHASE IS LIQUID

SPECIFIED TEMPERATURE K 323.000

SPECIFIED PRESSURE N/SQM 101,325.

MAXIMUM NO. ITERATIONS 30

CONVERGENCE TOLERANCE 0.00010000


77/83



*** RESULTS ***

OUTLET TEMPERATURE K 323.00

OUTLET PRESSURE N/SQM 0.10132E+06

HEAT DUTY WATT -0.13983E+06

REACTION EXTENTS:

REACTION REACTION

NUMBER EXTENT

KMOL/SEC

1 0.10981E-02



STREAM SECTION

BOTTOM C6H6 CNB EXH2O H2O

-------------------------


78/83



STREAM ID BOTTOM C6H6 CNB EXH2O H2O

FROM : DIST ---- RSTO ---- ----

TO : ---- RSTO DECANTER DECANTER MIXER

SUBSTREAM: MIXED

PHASE: LIQUID LIQUID LIQUID LIQUID LIQUID

COMPONENTS: KMOL/SEC

C6H5NO2 1.0757-03 0.0 1.0981-03 0.0 0.0

H2SO4 7.3724-05 0.0 1.6427-03 0.0 0.0

H2O 3.1510-18 0.0 3.7193-03 3.0900-02 2.6212-03

HNO3 1.9992-11 0.0 3.9522-06 0.0 0.0

C6H6 3.6209-05 1.4224-03 3.2431-04 0.0 0.0

TOTAL FLOW:

KMOL/SEC 1.1857-03 1.4224-03 6.7884-03 3.0900-02 2.6212-03

KG/SEC 0.1424 0.1111 0.3888 0.5566 4.7222-02

CUM/SEC 1.4003-04 1.2713-04 3.2101-04 5.6022-04 4.7524-05

STATE VARIABLES:

TEMP K 478.8604 298.0000 323.0000 298.0000 298.0000

PRES N/SQM 1.0133+05 1.0133+05 1.0133+05 1.0133+05 1.0133+05

VFRAC 0.0 0.0 0.0 0.0 0.0

LFRAC 1.0000 1.0000 1.0000 1.0000 1.0000


79/83



SFRAC 0.0 0.0 0.0 0.0 0.0

ENTHALPY:

J/KMOL 2.7788+05 4.9107+07 -3.4075+08 -2.8569+08 -2.8569+08

J/KG 2312.1927 6.2866+05 -5.9481+06 -1.5858+07 -1.5858+07

WATT 329.4732 6.9851+04 -2.3132+06 -8.8279+06 -7.4887+05

ENTROPY:

J/KMOL-K -3.3127+05 -2.5267+05 -2.3857+05 -1.6272+05 -1.6272+05

J/KG-K -2756.4033 -3234.6200 -4164.5254 -9032.4484 -9032.4484

DENSITY:

KMOL/CUM 8.4673 11.1885 21.1467 55.1564 55.1564

KG/CUM 1017.6101 873.9777 1211.4430 993.6590 993.6590

AVG MW 120.1805 78.1136 57.2873 18.0152 18.0152



STREAM SECTION

H2SO4 HNO3 MIXACID ORGANIC SPA

------------------------------

STREAM ID H2SO4 HNO3 MIXACID ORGANIC SPA


80/83



FROM : ---- ---- MIXER DECANTER DECANTER

TO : MIXER MIXER RSTO DIST ----

SUBSTREAM: MIXED

PHASE: LIQUID LIQUID LIQUID LIQUID LIQUID


C6H5NO2 0.0 0.0 0.0 1.0757-03 2.2385-05

H2SO4 1.6427-03 0.0 1.6427-03 7.3724-05 1.5689-03

H2O 0.0 0.0 2.6212-03 2.4803-05 3.4595-02

HNO3 0.0 1.1021-03 1.1021-03 1.7738-07 3.7748-06

C6H6 0.0 0.0 0.0 3.1697-04 7.3479-06

TOTAL FLOW:

KMOL/SEC 1.6427-03 1.1021-03 5.3660-03 1.4914-03 3.6197-02

KG/SEC 0.1611 6.9444-02 0.2777 0.1648 0.7806

CUM/SEC 8.8976-05 4.5735-05 2.0328-04 1.4334-04 7.5076-04

STATE VARIABLES:

TEMP K 298.0000 298.0000 298.0000 298.0000 298.0000

PRES N/SQM 1.0133+05 1.0133+05 1.0133+05 1.0133+05 1.0133+05

VFRAC 0.0 0.0 0.0 0.0 0.0

LFRAC 1.0000 1.0000 1.0000 1.0000 1.0000

SFRAC 0.0 0.0 0.0 0.0 0.0

ENTHALPY:


81/83



J/KMOL -7.9337+08 -1.7338+08 -4.1804+08 -2.3457+07 -3.0743+08

J/KG -8.0891+06 -2.7516+06 -8.0755+06 -2.1217+05 -1.4254+07

WATT -1.3032+06 -1.9108+05 -2.2432+06 -3.4984+04 -1.1128+07

ENTROPY:

J/KMOL-K -3.3300+05 -3.1260+05 -2.3701+05 -3.7927+05 -1.6879+05

J/KG-K -3395.2154 -4960.9513 -4578.3531 -3430.5411 -7826.0507

DENSITY:

KMOL/CUM 18.4618 24.0968 26.3970 10.4047 48.2138

KG/CUM 1810.7264 1518.4146 1366.4855 1150.2998 1039.8510

AVG MW 98.0794 63.0128 51.7666 110.5555 21.5674



STREAM SECTION

TOP

---

STREAM ID TOP

FROM : DIST

TO : ----

SUBSTREAM: MIXED


82/83



PHASE: LIQUID


C6H5NO2 0.0

H2SO4 0.0

H2O 2.4803-05

HNO3 1.7736-07

C6H6 2.8076-04

TOTAL FLOW:

KMOL/SEC 3.0574-04

KG/SEC 2.2389-02

CUM/SEC 2.6121-05

STATE VARIABLES:

TEMP K 324.4181

PRES N/SQM 1.0133+05

VFRAC 0.0

LFRAC 1.0000

SFRAC 0.0

ENTHALPY:

J/KMOL 2.6883+07

J/KG 3.6711+05

WATT 8219.1914

ENTROPY:


83/83

Documents

Simulation of Manufacturing Process of Nitrobenzene