• Study Resource
• Explore

Survey

* Your assessment is very important for improving the work of artificial intelligence, which forms the content of this project

Document related concepts

Stoichiometry wikipedia, lookup

Rate equation wikipedia, lookup

Chemical thermodynamics wikipedia, lookup

Fluid dynamics wikipedia, lookup

Vapor–liquid equilibrium wikipedia, lookup

Navier–Stokes equations wikipedia, lookup

Catalytic reforming wikipedia, lookup

Chemical plant wikipedia, lookup

Detailed balance wikipedia, lookup

River engineering wikipedia, lookup

Flash reactor wikipedia, lookup

Transcript
```CHEE 221: Chemical Processes and Systems
Module 1. Material Balances: Single Process Units without Reaction (Felder & Rousseau Ch 4.1‐4.3)
General Material Balance Equation (“GMBE”)
Accumulation = In – Out + Generation – Consumption
system boundary
Input streams to system
System over which mass balance is made
output streams from system
Accumulation within the system (mass buildup)
=
Input through system boundary
+
CHEE 221
‐
Generation within the system
Output through system boundary
‐
Consumption within the system
2
What is the System?
CHEE 221
3
Some Basic Process Unit Functions
 Splitter – divides a single input into two or more outputs of the same composition (no reaction)
splitter
 Mixer – combines two or more inputs (usually of different compositions) into a single output) (no reaction)
mixer
 Separator – separates a single input into two or more outputs of different composition (no reaction)
separator
CHEE 221
4
Basic Process Unit Functions…cont’d
 Reactor – carries out a chemical reaction that converts atomic or molecular species in the input to different atomic or molecular species in the output  Heat exchanger – transfers heat from one input to a second input (no reaction)
 Pump – changes the pressure of an input to that of the corresponding output (no reaction)
reactor
heat exchanger
pump
Actual process units can combine these different functions into a single piece of
hardware, and are given different names, e.g. a separator can be a distillation
column, a filter press, a centrifuge, etc.
F&R Encyclopedia of Chemical Engineering Equipment ( textbook website)
CHEE 221
5
Steam Boiler
Steam Boiler
CHEE 221
Heat Exchanger (no reaction)
+ Reactor (reaction)
6
Distillation—A Very Common Separation Process
CHEE 221
7
Material (Mass) Balances (“MBs”)‐No Reaction
A material balance is simply an accounting of material. For a given system in
which no reaction is occurring (you will not be told this, and will need to
know this from the type of unit that is under consideration; crystallizer,
evaporator, filter, furnace, etc.), a material balance can be written in terms of
the following conserved quantities:
1.
2.
3.
Total mass (or moles)
Mass (or moles) of a chemical compound
Mass (or moles) of an atomic species
To apply a material balance, you need to define the system and the quantities of
interest (e.g. mass of a component, total mass, moles of an atomic species).
What is your system, and what are you keeping track of?
System – a region of space defined by a real or imaginary closed envelope (envelope = system boundary) – may be a single process unit, collection of process units or an entire process
CHEE 221
8
Process Classification
Before writing a material balance (MB) you must first identify the type of process in question.
 Batch – no material (mass) is transferred into or out of the system over the time period of interest (e.g., heat a vessel of water)
 Continuous – material (mass) is transferred into and out of the system continuously (e.g., pump liquid into a distillation column and remove the product streams from top and bottom of column)  Semibatch – any process that is neither batch nor continuous (e.g., slowly blend two liquids in a tank)  Steady‐State – process variables (i.e., T, P, V, flow rates) do not change with time
 Transient – process variables change with time
CHEE 221
F&R Ch 4.1
9
F&R Example 4.1
Classify the following processes as batch, continuous, or
1.
2.
3.
4.
A balloon is filled with air at a steady rate of 2 g/min.
A bottle of milk is taken from the refrigerator and left on the kitchen table. Water is boiled in an open flask.
Carbon monoxide and steam are fed into a tubular reactor at a steady rate
and react to form carbon dioxide and hydrogen. Products and unused
reactants are withdrawn at the other end. The reactor contains air when
the process is started up. The temperature of the reactor is also constant,
and the composition and flow rate of the entering reactant stream are also
independent of time. Classify the process (a) initially and (b) after a long
period of time has elapsed.
CHEE 221
10
Material Balance Simplifications
The following rules may be used to simplify the material balance equation: Accumulation = In – Out + Generation – Consumption
 If the system is at steady‐state, set accumulation = 0
 In – Out + Generation – Consumption = 0
 If the balanced quantity is total mass, set generation = 0 and consumption = 0 (law of conservation of mass)
 Accumulation = In – Out
 If the balanced substance is a nonreactive species, (neither a reactant nor a product) or for non‐reacting systems in general, set generation = 0 and consumption = 0
 Accumulation = In – Out
CHEE 221
11
Problems Involving Material Balances
 Initial procedures will be outlined for solving single unit processes
– No reaction (consumption = generation = 0)
– Continuous steady‐state (accumulation = 0)
– And so the Conservation Equation becomes….. (what?)
 These procedures will form the foundation for more complex problems involving multiple units and processes with reaction  Following a standard methodology to solve problems is the key to success. This standard methodology will be illustrated via many examples in class, and is the one used by F&R.
CHEE 221
12
Example 1
450 kmol per hour of a mixture of n‐butanol and iso‐butanol containing 30
mole % n‐butanol is separated by distillation into two fractions. The flow rate
of n‐butanol in the overhead stream is 120 kmol/h and that of iso‐butanol in
the bottom stream is 300 kmol/h. The operation is at steady‐state.
Calculate the unknown component flow rates in the output streams. What is
the mole fraction of n‐butanol in the bottom stream? What is the mass
fraction?
CHEE 221
13
Fractionation of Oil
Wk 2 pre‐tutorial exercise:
Draw a schematic of a plate
(or tray) distillation column
(continuous operation), and
briefly explain how separation
occurs
F&R Encyclopedia of Chemical Engineering Equipment
(textbook website)
CHEE 221
14
Material Balance Procedures
All material balance calculations are variations on a single theme: Given values of some input and output stream variables (e.g. flowrates,
compositions), derive and solve equations for the others
Solving the equations is a matter of simple algebra (the math is easy!), however, you first need to:  convert the problem statement into a process flow diagram; what are the streams in/out and what components are in each stream?
 label the PFD with the ‘knowns” (flows, compositions, etc.), assign variables to the unknowns (remaining flows, compositions), identify the system on which you are doing the MB, and decide on your basis (mass/moles/input/output….)
 derive the necessary equations from the component and/or overall MB equations, and process constraint (PC) equations
 follow the standard methodology to solve the problem
CHEE 221
15
Process Flow Diagrams
A flowchart, or process flow diagram (PFD), is a convenient (actually,
necessary) way of organizing process information for subsequent
calculations.
To obtain maximum benefit from the PFD in material balance calculations, you must:
1. Write the values and units of all known stream variables (flows and compositions) at the locations of the streams on the chart. 2. Assign algebraic symbols to unknown stream variables (flows and compositions) and write these variable names and their associated units on the chart.
Your PFD is an essential part of the problem solution,
and will be assigned marks for completeness.
CHEE 221
F&R Ch 4.3a, Example 4.3‐1
16
Note on Notation
The use of consistent notation is generally advantageous. For the purposes of this course, the notation adopted in Felder and Rousseau will be followed. For example: n – moles
m – mass
n – molar flow rate
m – mass flow rate
V – volume
V – volumetric flow rate
x – component fractions (mass or mole) in liquid streams
y – component fractions in gas streams
CHEE 221
17
Example 2
A spent sulfuric acid solution is brought up to strength for a pickling process
in a mixer. Spent solution at 3% sulfuric acid (by weight) is mixed with a 50%
solution (by weight) to obtain the desired product concentration of 40% acid
by weight. All are aqueous solutions. Determine all flowrates on the basis of
100 lbm/h of product. If the actual flow of the spent stream is 300 lbm/h, what
must the flowrates of the streams be?
CHEE 221
18
Basis of Calculation
Basis of calculation – is an amount or flow rate of one of the process streams on a mass or mole basis
 If a stream amount or flow rate is given in the problem statement, use this as the basis of calculation (usually)
 If no stream amounts or flow rates are known, you can assume one, preferably a stream of known composition
– if mass fractions are known, choose a total mass or mass flow rate of that stream (e.g., 100 kg or 100 kg/h) as a basis
– if mole fractions are known, choose a total number of moles or a molar flow rate
CHEE 221
19
Flowchart Scaling
Scaling – the process of changing the values of all stream amounts or flow
rates by a proportional amount while leaving the stream compositions and
conditions unchanged.
 Scaling up – final stream quantities are larger than the original quantities
 Scaling down – final stream quantities are smaller than the original quantities
30 mol A/min
70 mol B/min
40C, 1 atm
100 mol/min
0.30 mol A/mol
0.70 mol B/mol
40C, 1 atm
CHEE 221
60 mol A/min
140 mol B/min
Scale up process by a factor of 2
40C, 1 atm
200 mol/min
0.30 mol A/mol
0.70 mol B/mol
40C, 1 atm
20
Methodology for Solving Material Balance Problems
1. Choose a basis of calculation (input, output, mass, moles)
2. Draw and fully label a flowchart with all the known and unknown process variables (flows, compositions) as well as the basis of calculation. Be sure to include units.
3. Write any Process Constraint (PC) equations that relate variables.
4. Determine the number of unknowns and the number of equations that can be written to relate them. That is, does the number of equations equal the number of unknowns?
5. Solve the equations 6. Check your solution – does it make sense? Calculate the quantities requested in the problem statement if not already calculated
7. Cleary present your solution with the proper units and the correct number of significant figures “Understanding the Concepts” is not good enough. You will not be
tested on “Understanding the Concepts”. You will be tested on your
ability to set up and solve problems, and to get the correct answer.
CHEE 221
21
Example 3: Quiz 1 2007
A mixture containing 42 wt% benzene (B) and 58 wt% toluene (T) is fed to a
distillation column at a flowrate of 100 kg/min. The product stream leaving the
top of the column (the overhead product) contains 90 wt% benzene, and 85
wt% of the total benzene fed to the column exits in this overhead product
stream.
Calculate the mass flowrate and mass composition of the product stream
leaving the bottom of the column. Calculate the volumetric flowrate of the
overhead product, assuming that it exits the distillation column as a vapour
stream at 82 ºC and 1 atm (abs).
Physical Property Data (S.G.=specific gravity) from Table B1:
• Benzene
S.G.=0.879
MW=78.11 g/mol
• Toluene
S.G.=0.866
MW=92.13 g/mol
• Water
density = 1.00 kg/L
MW=18.02 g/mol
R = 0.08206 L∙atm/(mol∙K)
CHEE 221
22
Degrees of Freedom Analysis: A Motivating Example
A feed stream containing C8 and C10 hydrocarbons is split into 3 product
streams: an overhead fraction, a middle cut and a bottom fraction, whose
mole fraction compositions are shown below. Seventy per cent of the C8
entering the column in the feed is recovered in the overhead. On the basis
of 100 lb‐moles/h of feed determine the molar flow rates of the 3 product
streams.
C8: 0.516
C10: 0.484
100 lb‐moles/h
C8: 0.300
C10: 0.700
CHEE 221
C8: 0.352
C10: 0.648
C8: 0.146
C10: 0.854
23
Independent Equations
A set of equations are independent if you cannot derive one by adding and subtracting combinations of the others.
x  2y  z 1
Is this set of equations independent? 2x  y  z  2
y  2z  5
1 2 1   x   1 
2 1  1  y   2
   

0 1 2   z  5
1 0 0  x   6 
0 1 0  y    5

   
0 0 1  z   5 
row
reduce
Rank = 3. No non‐zero rows in reduced form
CHEE 221
24
Independent Equations… cont’d
Are these sets of equations independent?
x  2y  z 1
2 y  4 z  10
y  2z  5
x  2y  z 1
2x  y  z  2
3x  3 y  3
CHEE 221
25
Degree‐of‐Freedom Analysis
A degree‐of‐freedom analysis (DFA) is a determination of the number of
unknowns in a problem, and the number of independent equations that can
be written. The difference between the number of unknowns and the number
of independent equations is the number of degrees‐of‐freedom, DF or ndf, of
the process.
ndf  nunknowns  nindependent equations
Possible outcomes of a DFA: – ndf = 0, there are n independent equations and n unknowns. The problem can be solved. – ndf > 0, there are more unknowns that independent equations. The problem is underspecified. ndf more independent equations or specifications are needed to solve the problem.
– ndf < 0, there are more independent equations than unknowns. The problem is overspecified with redundant and possibly inconsistent relations. CHEE 221
26
DFA: Sources of Equations
Sources of equations that relate unknown process variables include: 1. Material balances – for a nonreactive process, usually but not always, the maximum number of independent equations that can be written equals the number of chemical species in the process
2. Process constraints– given in the problem statement
3. Physical constraints – e.g., mass or mole fractions must add to 1 (usually taken care of when setting up PFD)
4. Stoichiometric relations – systems with reaction (later)
5. Energy balances – 2nd half of course
CHEE 221
27
Notes on DFA: Dependent Material Balances
There are two common situations where you will find fewer independent equations than species, and they are:
1.
Balance around a splitter
– Single input – two or more outputs with same composition
– Only 1 independent balance equation, since:
m1 = m2 + m3
(Overall Balance)
and x1m1 = x2m2 + x3 m3
(Balance on A)
but since x1 = x2 = x3, these balances are not independent
– Splitters are used for:
• Purge streams (reactor systems with recycle)
• Total condensers at the top of distillation columns
m1 kg/h
x1 kg A/kg
(1‐x1) kg B/kg
CHEE 221
m2 kg/h
x2 kg A/kg
(1‐x2) kg B/kg
Splitter
m3 kg/h
x3 kg A/kg
(1‐x3) kg B/kg
28
Notes on DFA: Dependent Material Balances… cont’d
Distillation Column with Total Condenser
CHEE 221
29
Notes on DFA: Dependent Material Balances… cont’d
2. If two species are in the same ratio to each other wherever they appear in
a process and this ratio is incorporated in the flowchart labeling, balances
on those species will not be independent equations.
– Situation occurs frequently when air is present in a nonreactive
process (21 mol% O2; 79 mol% N2)
– E.g., vapourization of liquid carbon tetrachloride into an air stream
CHEE 221
n1 mol O2/s
3.76n1 mol N2/s
n3 mol O2/s
3.76n3 mol N2/s
n4 mol CCl4(v)/s
n2 mol CCl4(L)/s
n5 mol CCl4(L)/s
Best to treat air as a single species in this situation
30
Summary: MB applied to single process units without reaction
•
Standard procedures was developed for single‐unit processes (F&R 4.3)
– No reaction (Consumption=Generation=0)
•
Develop good habits now, and practice. Problems will get more complex as we extend the procedures to multiple‐unit processes (starting in ≈Week 3) and processes with reaction (starting in Week 4/5)
•
Standard procedures are summarized in F&R Section 4.3 and include:
– drawing/labeling a process flow diagram (4.3a)
These are critical sections
– selecting a basis of calculation (4.3b)
of the text and
– setting up material balances (4.3c)
form the basis for Quiz 1
– performing a degree of freedom analysis (4.3d)
CHEE 221
31
Example 4
Hot soap is chilled on a roller and scraped continuously from the roller onto a moving
conveyor belt which carries the soap into a dryer (see below). The entering soap
contains 25% water by weight. It is desired to reduce the water content to 15% by
weight and to produce 1200 lb/h of nearly dry soap chips. The entering air contains
0.3 mole % water vapour. The dryer manufacturer suggests that the dryer operates
efficiently when the nearly dry air/wet soap flow ratio is 3.0. Calculate the unknown
flowrates and compositions. Air is 21% oxygen and 79% nitrogen (mole basis) and has
a molecular weight of 29.0 g/mol.
moist air
hot, nearly dry air
Soap Dryer
wet soap chips
CHEE 221
dried soap chips
32
Condensers and Evaporators
Wk 3 pre‐tutorial exercise:
Dryers and dehumidifiers are
two examples of a general
class of separators known as
condensers.
Look into the difference
between condensers and
evaporators, and explain their
industrial usage. Can you think
of a household example of an
evaporator?
F&R Encyclopedia of Chemical Engineering Equipment
(textbook website)
CHEE 221
33
Example F&R 4.3‐1
An experiment on the growth rate of certain organisms requires an
environment of humid air enriched in oxygen. Three input streams are fed
into an evaporation chamber to produce an output stream with the desired
composition.
A: Liquid water, fed at a rate of 20.0 cm3/min
B: Air (21 mole% O2, the balance N2)
C: Pure oxygen, with a molar flow rate one‐fifth of the molar flow rate of stream B. The output gas is analyzed and is found to contain 1.5 mole% water. Draw
and label a PFD, and calculate all unknown stream variables (i.e. flows and
compositions).
Work through on your own, then check with solution in the textbook
CHEE 221
34
Example: Quiz 1 2009
A continuous distillation column is to be used to separate a 3‐component mixture of
acetic acid (AA), water (W) and Benzene (B), and a trial run gave the data below (mass
basis). The data for the benzene in the feed (which consists of AA, W and B) was not
taken because of an instrument malfunction. Use a degree of freedom analysis, and
then calculate the benzene flow in the feed in kg/h.
Waste
10.9% AA
21.7% W
67.4% B
Aqueous Solution
(containing 80% AA + 20% W)
+
B (data not available)
Product
350 kg/h pure AA
Answer: B in feed = 311 kg/h
CHEE 221
35
```
Related documents