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Design Of A Sulfuric Acid Production Plant Engineering Essay

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Any opinions, findings, conclusions or recommendations expressed in this material are those of the authors and do not necessarily reflect the views of UK Essays.

This project is prepared according to the requirements of chemical engineering department, and it's also a preliminary study of sulfuric acid production plant.

The project begins with chapter one which includes introduction, definition of sulfuric acid and shows the main uses of sulfuric acid which have made it an important chemical in the world, followed by chapter two which talks about literature, market survey and the history and current processes for production the sulfuric acid also it gives small glimpse of the prices trends of the raw material and product.

That is followed by description for various processes to produce sulfuric acid in chapter three, which ends with the selection of the best process which is the double contact process; the description and flow sheet of the selected process are discussed in chapter four.

Material and energy balance results are listed in chapter five and the location of the plant is selected in chapter six by comparing different locations, and the best location for the plant (as its set in this report) is Aqaba city. .

Finally, material and energy balance details are discussed in the appendix, that includes the used charts and references.

CHAPTER ONE

INTRODUCTION

1.1 Definition

Sulfuric acid is a strong mineral acid with the molecular formula H2SO4. It is a clear, colorless, odorless, viscous liquid that is very corrosive. It is soluble in water at all concentrations. Sulfuric acid has many applications, and is one of the top products of the chemical industry.

There are another names for sulfuric acid, it is sometimes called oil of vitriol.1

Its chemical formula is

Figure (1.1.1): Sulfuric Acid Formula1

1.2 Physical and Chemical properties

This table shows the main chemical and physical properties of sulfuric acid

Sulfuric acid

IUPAC

Oil of vitriol

Other name

H2O4S

Molecular formula

98.08 g mol−1

Molar mass

Clear, colorless, odorless liquid

Appearances

1.84 g/cm3, liquid

Density

10 °C, 283 K, 50 °F

Melting point

337 °C, 610 K, 639 °F

Boiling point

Miscible

Solubility in water

−3

Acidity(pka)

pungent odor

Odor

Non-flammable

Flash point

26.7 cP (20 °C)

Viscosity

0.3

Ph

Table (1.2.1): physical properties1

1.3 Application and Uses

Sulfuric acid is a very important chemical commodity, and indeed, a nation's sulfuric acid production is a good indicator of its industrial strength.

It is used as electrolyte in lead-acid batteries (accumulators) .

It is important in the production of fertilizers such as ammonium sulfate (sulfate of ammonia), (NH4)2SO4, and superphosphate, Ca(H2PO4)2, which is formed when rock phosphate is treated with sulfuric acid.

It is used to remove oxides from iron and steel before galvanising or electroplating .

Concentrated sulfuric acid is used as a dehydrating agent, that is, to remove water, since it has a tendency to form hydrates such as H2SO4.H2O, H2SO4.2H2O.

Sulfuric acid is used in the production of nitroglycerine, an inorganic ester & organic nitrate, which is used as an explosive.

It is used in petroleum refining to wash impurities out of gasoline and other refinery products.

It is used in manufacturing of hydrochloric acid, nitric acid, phosphoric acid, ether, plastics, metal sulfates, cellophane, dyes, drugs, perfumes, disinfectants and even glue.1

This chart shows the distribution of using sulfuric acid

Figure (1.3.1): Sulfuric Acid Distribution.1

Specification of raw materials

sulfur, S, 16

Name, symbol, number

32.065g·mol−1

Standard atomic weight

Yellow colored lumps, crystals, powder, or formed shape

Appearances

Lumps 75-115 lbs./ft3 Powder 33-80 lbs./ft3

Bulk Density

388.36 K, 115.21 °C, 239.38 °F

Melting point

717.8 K, 444.6 °C, 832.3 °F

Boiling point

Insoluble

Solubility In Water

Solid

Physical State

1.819 g·cm−3

Liquid density at maps.

Table (1.3.1): Physical & Chemical Properties of Sulfur.1

CHAPTER TWO

LITERATURE AND

MARKET SURVEY

2.1 History and Current processes

The discovery of sulfuric acid is credited to the 8th century chemist and alchemist, Jabir ibn Hayyan (Geber). The acid was later studied by 9th century Persian physician and alchemist Ibn Zakariya al-Razi (Rhazes), who obtained the substance by dry distillation of minerals including iron(II) sulfate heptahydrate, FeSO4·7H2O, and copper(II) sulfate pentahydrate, CuSO4·5H2O. When heated, these compounds decompose to iron(II) oxide and copper(II) oxide, respectively, giving off water and sulfur trioxide, which combine to produce a dilute solution of sulfuric acid. 1

This method was popularized in Europe through translations of Arabic and Persian treatises, as well as books by European alchemists, such as the 13th-century German Albertus Magnus.1

There are two major processes (lead chamber and contact) for production of sulfuric acid and it is available commercially in a number of grades and concentrations. The lead chamber process, the older of the two processes, is used to produce much of the acid used to make fertilizers; it produces a relatively dilute acid (62%-78% H2SO4). The contact process produces a purer, more concentrated acid but requires purer raw materials and the use of expensive catalysts. n both processes sulfur dioxide is oxidized and dissolved in water. The sulfur dioxide is obtained by burning sulfur, by burning pyrites (iron sulfides), by roasting nonferrous sulfide ores preparatory to smelting, or by burning hydrogen sulfide gas. Some sulfuric acid is also made from ferrous sulfate waste solutions from pickling iron and steel and from waste acid sludge from oil refineries. 1

2.2 Supply and Demand

This table shows the production rates of sulfuric acid (in metric tones) in some countries at different years.

Production of sulfuric acid in metric tones

Year

country

1994

1997

2000

2006

France

2227

2242

2269

1755

Germany

3380

3496

4898

4595

Greece

360

675

688

815

Italy

1228

1590

1043

1616

Spain

2348

2810

2418

3500

United kingdom

1225

1205

1058

447

Sweden

518

630

629

1010

Table (2.2.1): Production Rates of Sulfuric Acid.3

This table shows the production and sales amounts of sulfuric acid and the consumption rate of sulfur in Jordan from 2000 to 2005, these amounts in (ton/year).

Sulfur consumption

(ton/tear)

ٍSulfuric acid

Year

Sales

(ton/year)

Production

(ton/year)

370925

43824

1108605

2000

309816

46614

919548

2001

351011

43307

1055208

2002

265865

51445

961208

2003

364301

49661

1102899

2004

346345

48323

1046540

2005

Table (2.2.2)Jordan Production, Sales and Raw Material Consumption.5

2.3 Prices trends of the raw material and product

The global sulfuric acid market experienced an unprecedented rise and fall in pricing between fall 2007 and spring 2009. Consumption of sulfuric acid for fertilizers fell steeply in the second half of 2008 due to the collapse in the global economy. The second half of 2009 is expected to experience almost flat to slightly positive growth, anticipating the improvement in market conditions in 2010. Trade is expected to fall globally, except for Southeast Asia, which would continue to depend on imports. As of early spring 2009, the market is continuing to deteriorate as the supply shortage situation has been replaced by product oversupply in almost all regions.

And the world sulfuric acid supply trends are shown in the following chart.

Figure (2.3.1): World Sulfuric Acid Supply.2

CHAPTER THREE

PROCESS SELECTION

Process Selection

Sulfuric acid is an important raw material used in many industrial processes, such as phosphate fertilizer production and to a much lesser extent for nitrogen and potassium fertilizers, sulfuric acid is produced by catalytic oxidation of sulfur dioxide to sulfur trioxide, which is subsequently absorbed in water to form sulfuric acid.

There are no major variations of commercial interests on this mentioned chemistry. There are alternatives as to source of Sulfur dioxide and method of conversion to sulfur trioxide. The two most common methods for the conversion of sulfur dioxide to sulfuric

acid are:

1. Lead Chamber Process.

2. Contact Process

3.1 Lead Chamber Process

This is an old process and was introduced in Europe in near the middle of 18th century, it's used to produce much of the acid used to make fertilizers; it produces a- relatively dilute acid (62%-78% H2SO4).The classic lead chamber process consists of three stages: Glover tower, lead chambers and Guy-Lussac Tower.

In this method hot sulfuric dioxide gas enters the bottom of the reactor called a Glover tower where it is washed with nitrous vitriol (sulfuric acid with nitric oxide, NO, and nitrogen dioxide, NO2, dissolved in it) and mixed with nitric oxide and nitrogen dioxide gases.

The Glover tower serves two functions: concentration of the chamber acid and stripping of nitrogen oxides from the liquid to the gas. Concentration of the chamber acid (62% to 68% H2SO4) is achieved by the hot gases entering the tower which evaporate water from the acid.

Some of the sulfur dioxide is oxidized to sulfur trioxide and dissolved in the acid wash to form tower acid or Glover acid (about 78% H2SO4). The dissolved nitrogen oxides are stripped from the acid and carried with the gas out of the Glover tower into the lead chambers.

From the acid tower a mixture of gases (including sulfur dioxide and trioxide, nitrogen oxides, nitrogen, oxygen, and steam) is transferred to a lead-lined chamber where it is reacted with more water.

Sulfuric acid is formed by a complex series of reactions; it condenses on the walls and collects on the floor of the chamber. There may be from three to twelve chambers in a series. The acid produced in the chambers, often called chamber acid or fertilizer acid, contains 62% to 68% H2SO4.

After the gases have passed through the chambers they are passed into a reactor called the Gay-Lussac tower where they are washed with cooled concentrated acid (from the acid tower); the nitrogen oxides and unreacted sulfur dioxide dissolve in the acid to form the nitrous vitriol used in the acid tower. Remaining waste gases are usually discharged into the atmosphere.

Product acid at a concentration of 78% H2SO4 is drawn from the cooled acid stream that is circulated from the Glover tower to the Guy-Lussac tower.  Nitrogen losses are made up with nitric acid which is added to the Glover tower.

The major disadvantage includes the limitations in throughput, quality and concentration of the acid produced, also the environmental pollution.

Figure (3.1.1): Typical process flow sheet for the lead Chamber.

3.2 Contact Process

Because of economic reasons Contact plants are widely used compared to the lead plants, they are classified according to the raw materials charged to them: elemental Sulfur burning, spent sulfuric acid and hydrogen sulfide burning, and metal sulfide ores and smelter gas burning. The contributions from these plants to the total acid production are 81, 8, and 11 percent, respectively.

The contact process incorporates three basic operations (stages), each of which corresponds to a distinct chemical reaction.

First, elemental sulfur is received in a solid form containing various impurities. The sulfur is melted in the sulfur melter in the presence of hydrated lime which neutralizes any acidity present in the sulfur. This neutralization prevents problems of acid corrosion which would otherwise be encountered.

Heat for the melting of the sulfur is supplied from steam coils. The molten sulfur is kept agitated to improve heat transfer, to prevent solids settling on the bottom of the sulfur pits and to prevent a crust forming on top. The "dirty sulfur" is filtered to remove impurities present and after filtering is transferred to the "clean sulfur" pit where it is kept molten until it is pumped to the burner.

Molten sulfur at a temperature of 130°C is sprayed into the burner in the presence of warm, dry air. The sulfur burns, forming sulfur dioxide

S + O2 € € € €  SO2 ∆H = -300 kJ mol-1

The resulting sulfur dioxide is fed to a process unit called a converter, where it is catalytically oxidized to sulfur trioxide (SO3):

2SO2 + O2 € € € € 2SO3 ΔH = -100 kJ mol-1

It's apparent that the equation gives a decrease in volume; this reaction would be aided by pressure. High conversions are however, obtainable with catalysts at 400 to 500oC with a small excess of oxygen and the use of pressure.

The available methods to maximize the formation of SO3:

As this is an exothermic process, a decrease in temperature by removal of the heat will favour the formation of SO3.

Increased oxygen concentration.

SO3 removal (as in the case of the double absorption process).

Increased pressure.

Catalyst selection, to reduce the working temperature (equilibrium).

Longer reaction time.

In the contact processes, the sulfur dioxide is converted to sulfur trioxide by the use of metal oxide catalyst, the characteristics of the used catalyst are:

Porous carrier having large surface area, controlled pore size and resistance to process gases at high temperature; in pellet form if used in fixed bed and

powdered form if used for fluidized bed. Ex- Alumina, silica gel, zeolites.

Active catalytic agent:

Preparations are generally kept secret for the competitive reasons but they usually

consist of adding water soluble compounds to gels or porous substrates and firing

at temperature below the sintering point.

Promoter:

Alkali and/or metallic compounds added in trace amounts to enhance the activity

of the catalytic agent.

A catalyst, vanadium pentoxide (V2O5) is used to increase the reaction rate because it's relatively immune to poisons, also because of its low initial investment and only 5% replacement per year. It is only effective above its melting point of 400 °C. The greatest conversion of SO2 to SO3 is reached by passing the gas over several catalyst beds, cooling the gas between each pass so that the reaction temperature remains between 400 and 500 °C. As can be seen the figure.

The disadvantages of using the V2O5 catalyst are that it must use dilute SO2 input (7-10%), as a catalyst it is less active and requires high oxygen or sulfur dioxide to give economic conversions also it requires larger converters and thus higher initial investment.

Finally, the sulfur trioxide is absorbed in to very concentrated sulfuric acid (a 98-99 percent solution of H2SO4 in water), This operation takes place in the absorbing tower where the gas travels up through the tower, counter-current to the acid falling from the top of the tower producing a thick fuming liquid called oleum, the oleum is mixed carefully with water to avoid producing fine mist of sulfuric acid that is difficult to condense and could escape to pollute the air, the sulfur trioxide in the oleum reacts with the water as follows:

SO3 + H2O € € € € € € € € H2SO4 ∆H = -200 kJ mol-1

It is clear that the reaction is exothermic and the absorbing sulfuric acid has to be cooled continuously; the heat is available at a relatively low temperature and is not worth recovering.

The efficiency of the absorption step is related to :

The H2SO4 concentration of the absorbing liquid. (98.5 - 99.5%).

The temperature range of the liquid (normally 70 -120 0C).

The technique of the acid distribution.

The raw gas humidity (mist passes the absorption equipment).

The mist filter.

The temperature of incoming gas.

The co-current or countercurrent character of the gas stream in the absorbing liquid.

Main disadvantages of the contact process are that concentrated acid (98%) of high purity can be produced directly and that compact plants of quite high capacity have now become rather common place.

The contact process can be applied in different techniques; three of those techniques are described in the following sections

3.2.1 Single contact / single absorption process

After purification and drying, the SO2 is converted to SO3 using a series of four catalyst beds, containing alkali and V2O5. Afterwards, the SO3 is absorbed in concentrated sulfuric acid and, if necessary, an oleum absorber is installed upstream. SO3 reacts with the water contained in the absorber acid to yield H2SO4. The absorber acid is kept at the desired concentration of approximately 99% w/w by addition of water or dilute H2SO4.

The single contact/single absorption process is generally used for gases with an SO2 Content from 3 - 6 %. New single contact plants are built only for inlet gases with substantial fluctuation of the SO2 content.

The investment cost of this technique is low compared to the investment cost of double contact plants.

Figure (3.2.1.1): Typical process flow sheet for a single catalysis plant.

3.2.2 Double Contact/ Double Absorption Process

The double contact process was implemented to develop the single contact/single absorption process. In this process a primary SO2 conversion of 85 - 95 % is achieved in the first catalysis stage of the converter before entry into an intermediate absorber, depending on the arrangement of the converter beds and the contact time.

What makes the double contact/double absorption process more advantageous is that its ability to feed gases with higher SO2 concentrations than would be possible with the single catalysis process. Which leads to smaller gas volumes and therefore smaller equipment with comparable production capacities.

This results in a considerably higher conversion rate, if the residual gas is passed through the following converter beds (usually one or two). The SO3 which is formed in the second catalysis stage is absorbed in the final absorber.

In general the process uses gases with an SO2 content of 10 t o11 %. The inlet gas temperature is about 4000C. Gases with lower temperatures require reheating from 50 to 4000C. This is usually carried out with recovered heats from the conversion process.

Operating the double contact process at an elevated pressure of 5 bar increases the conversion rate by shifting the conversion equilibrium and favouring the formation of SO3.

The disadvantages are higher electricity consumption and, at the same time, less steam production. Higher NOx emissions are caused by higher sulfur combustion temperatures (18000C), but savings of 10 -17 % on investment costs are gained.

Figure 3.2.2.1: Typical process flow sheet for a sulfur burning double catalysis

plant.

3.2.3 Wet catalysis process

The wet catalysis process is applicable to wet SO2 gases. The potential for the formation of sulfuric acid mist might require tail gas treatment.

Wet SO2 gases (eg. from the burning of H2S gases or from the catalytic conversion of H2S gases) are directly supplied into the contact tower without previous drying. SO3 formed by the catalytic conversion immediately reacts with the moisture of the gases, thereby forming the acetic acid. The sulfuric acid is condensed in a condenser installed after the contact tower.

Factors

Sulfuric Acid Production By Lead Chamber process

Sulfuric Acid Production By single contact/single absorption process

Sulfuric Acid Production By double contact/double absorption process

Sulfuric Acid Production By Wet Catalysis process

Health and safety hazards involved

Less safe, waste gases are discharged to the atmosphere

Less amount of SO3 is absorbed so the rest is discharged to the atmosphere

A larger amount of SO3 is absorbed

A larger amount of SO3 is absorbed

Operating cost

High operating cost

Less operating

The least operating cost

Less operating cost

Raw material

SO2, NO, NO2, O2, H2O.

Melted sulfur, O2, SO2, SO3.

Melted sulfur, H2O, O2, SO2, SO3.

Wet SO2 gases, H2S, O2, SO3.

Waste products and by products

Exhaust gases are discharged to the atmosphere

Large amounts of SO2 gas are discharged to the atmosphere

Less amounts of SO2 gas are discharged to the atmosphere, less heat released after each successive catalyst bed.

A larger amount of SO3 is absorbed

Equipment

Acid Tower (Glover Tower), Lead Chambers, Reactor (Gay-lussac Tower)

Air dryer, burner, waste heat boiler, converter, single absorption column.

Air dryer, burner, waste heat boiler, converter, intermediate and external absorption column.

Burner, convertor, acid tower.

Yield

Yields 78% H2SO4

New plants achieve 98 to99 % conversion rates

Yields about 98%

Yields 70 to 80 % H2SO4 

Environmental pollution

More gases are discharged to the atmosphere

More gases discharged to the atmosphere

Less gases discharged to the atmosphere

More gases are discharger to the atmosphere

Purity of products

Low purity

Low purity

High purity

Low purity

Table (3.2.1): Process selection

Factors

Sulfuric Acid Production By Lead Chamber process

Sulfuric Acid Production By single contact/single absorption process

Sulfuric Acid Production By double contact/double absorption process

Sulfuric Acid Production By Wet Catalysis process

Health and safety hazards involved

5

5

5

3

Operating cost

6

4

7

5

Raw material

6

5

7

5

Waste products and by products

6

6

7

5

Equipment

7

5

8

6

Yield

5

6

7

9

Environmental pollution

5

5

6

4

Purity of products

6

5

7

9

Total (80)

46

41

54

46

Table (3.2.2): Process Selection

According to the discussion and the data presented above we choose the Double Contact/Double Absorption process.

CHAPTER FOUR

PROCESS DISCRIPTION

4.1 Production of H2SO4 by double contact process

The process begins in the burner, in which the melt sulfur is pumped to the burner where it is burnt in an excess of dry air. The gas exiting the burner is maintained at (8 - 9%v/v) sulfur dioxide and approximately 830°C due to the heat produced by the exothermic reaction.

Sulfurs on burning gives about one third of heat combustion of coal ,and this heat raises the temperature of combustion gases roughly in accordance with the figure (4.1.1) as shown.

Figure (4.1.1): Theoretical Flame Temperature.8

This heat is high in temperature and there is plenty of it, consequently it is worth utilizing and the hot gases are led across pipes through which the water passes. The water is heated, steam is raised and the gases are cooled.

The sulfur dioxide/air gas mixture is then passed through the stream to converter. The sulfur dioxide is converted to sulfur trioxide by reacting with oxygen over a catalyst.

This reaction is described by the equation:

2SO2 + O2 € € € € 2SO3 ΔH = -100 kJ mol-1

This reaction occurs in the converter, a four-stage reaction vessel with each stage consisting of a solid catalyst bed through which the gas is passed. The catalyst used is vanadium pentoxide (V2O5), and potassium sulphate dispersed on a silica base which forms a porous support, giving a large surface area for reaction.

This reaction is exothermic and its equilibrium constant decreases with increasing temperature (Le Chatelier.s Principle).

Figure (4.1.2) shows the percentage conversion of SO2 to SO3 that would be reached at an SO2 concentration of 8% v/v and a range of gas temperatures.

However, the reaction rate is also temperature dependent, so that if the temperature becomes too low the equilibrium point will not be reached.

In practice, the gas temperature must be maintained between (400 - 500°C) to maintain a high reaction rate and also high conversion equilibrium.

As the reaction is exothermic, heat is generated across each of the catalyst beds. This heat must be removed between each stage to maintain the optimum reaction temperature into the following stage. The temperature rise through each catalyst bed and the inter-stage cooling is shown in Figure (4.1.2).

Figure (4.1.2): The Temperature Rise Through Beds.7

The gas after passing through three catalyst bed goes to the first absorption tower where the Sulfur trioxide is removed. The gas is then reheated to about 420 C, passed through the fourth catalyst bed, then cooled and sent to a second absorption tower.

The gas mixture goes to the first and second absorption tower, a packed tower where SO3 is absorbed into a counter-current flow of 98 - 99% sulfuric acid.

The overall reaction can be described by the following equation, where sulfur trioxide reacts with the free water to produce sulfuric acid:

SO3 + H2O € € € € € € € € H2SO4 ∆H = -200 kJ mol-1

The circulating sulfuric acid must be maintained at about 98% concentration and temperature is controlled in the desired rang of (70°C_90°C) to maximize the absorption efficiency.

The acid strength is important because the vapor pressure of sulfur trioxide above sulfuric acid is at a minimum at an acid strength of 98% (see Figure (4.1. 3)).

At higher concentrations the increased vapor pressure is caused by SO3 and at lower concentrations the water vapor pressure increases sharply and the resultant acid mist is not readily re-absorbed and escapes to the atmosphere. A stream of sulfuric acid is continuously bled off and cooled through a plate heat exchanger before being passed into the storage tanks.

Figure (4.1.3): Relation Between Vapor Pressure and Concentration.7

Figure (4.1.4) : Flow Sheet

CHAPTER FIVE

ENERGY AND MASS BALANCE

5.1 MASS BALANCE

*Drier:

Components

Amount

%

H20

1.27

1.3

O2

21.12

23

N2

69.4

75.7

Temperature

25C

pressure

1 atm

M1

M2

Components

Amount

%

H2SO4

39.4

98

H2O

0.8

2

Temperature

150C

pressure

1 atm

M3

Components

Amount

%

O2

21.12

23.3

N2

69.4

76.7

Temperature

25C

pressure

1 atm

M4

Components

Amount

%

H2SO4

39.42

95

H2O

2.1

5

Temperature

150C

pressure

1 atm

*Burner:

M3

Components

Amount

%

O2

21.12

23.3

N2

69.4

76.7

Temperature

26C

 

pressure

1 atm

 

M5

Components

Amount

%

S

3.76

100

Components

Amount

%

SO2

28.16

29

O2

7.04

7

N2

69.4

64

Temperature

830C

 

pressure

1 atm

 M6

*Converter:

M6

Components

Amount

%

SO2

28.16

29

O2

7.04

7

N2

69.4

64

Temperature

400C

pressure

1 atm

M7

Components

Amount

%

O2

2.11

2

N2

69.44

66

SO2

8.45

8

SO3

24.64

24

Temperature

450

pressure

1 atm

M8

Components

Amount

%

SO2

26.72

26

O2

1.69

1.6

N2

69.44

66.4

SO3

26.72

26

Temperature

450

pressure

1 atm

M9

Components

Amount

%

SO2

0.314

6

O2

0.0768

1.5

N2

3.47

66.5

SO3

1.36

26

Temperature

450

pressure

1 atm

M10

Components

Amount

%

SO2

0.314

6

O2

0.0768

1.5

N2

3.47

66.5

SO3

1.36

26

Temperature

450

pressure

1 atm

M11

Components

Amount

%

SO2

6.08

6

O2

1.54

6

N2

65.97

66.5

SO3

25.84

26

Temperature

450

pressure

1 atm

*Internal absorption column:

M11

Components

Amount

%

SO2

6.08

6

O2

1.54

6

N2

65.97

66.5

SO3

25.84

26

Temperature

450

pressure

1 atm

M13

Components

Amount

%

SO2

6.08

0.63

O2

1.54

0.16

N2

65.97

7.21

H2SO4

892.45

92

Temperature

450

pressure

1 atm

M12

Components

Amount

%

H2SO4

601.43

95

H2O

5.81

5

Temperature

150C

pressure

1 atm

External absorption column:

M10

Components

Amount

%

SO2

0.314

6

O2

0.0768

1.5

N2

3.47

66.5

SO3

1.36

26

Temperature

450

pressure

1 atm

M14

Components

Amount

%

H2SO4

32.66

95

H2O

0.31

5

Temperature

150C

pressure

1 atm

M15

Components

Amount

%

SO2

6.08

10

O2

1.54

3

N2

3.47

6

H2SO4

54

81

Temperature

450

pressure

1 atm

The final stream for H2SO4 is M15+M13,which the total amount equal 937Kg/hr.

5.2 Energy balance:

Burner

Burner

Tin Tout

Tin = 250C

Tout = 8300C

heat of combustion of sulfur is = 9079.2*103 j/g

Moles of Sulfur burnt = 3.76 Kg/hr

Heat coming out of the reaction = 9079.2*103 * 3760 = 1.25 x 1011 J/hr

because this reaction is exothermic,

Q = - 1.212 x 1011 J/hr

Table ()

Comp

a

b

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

859888.6

428

28.16

805

19492641798

O2

175430

12281

113.92

26300019

428

7.04

805

1.49047*1011

N2

61.2899

80925

248

80065593

428

69.4

805

4.47302*1012

Waste heat boiler

Waste Heat Boiler

Tin Tout

Tin = 8300C

Tout = 4000C

Hin = 435473 J/hr

Table ()

Comp

A

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

860962.7

615

28.16

805

19516992263

O2

175430

12281

113.92

50815637

615

7.04

805

2.87982*1011

N2

61.2899

80925

248

1.44*108

615

69.4

805

8.02075*1012

Hout = 187347590 J/hr

Table ()

Comp

a

B

c

CP

Temperature

m

(Tin-25)

m*cp*(T-25)

SO2

857430

5.7443

860962.7

615

28.16

375

9091766582

O2

175430

12281

113.92

50815637

615

7.04

375

1.34153*1011

N2

61.2899

80925

248

1.44*108

615

69.4

375

3.73638*1012

Heat evolved from waste heat boiler = Hin - Hout - (- 1.212 x 1011)

= -1.21014* 1011 J/hr

Converter

H.E

H.E

H.E

Bed

2

Bed

3

Bed

4

Bed

1

Tin Tout

Bed (1):

T in =4000C

T out =6000C

Heat of reaction (∆Hrxn) = -100 KJ/mol

Heat evolved = h in - h out + ∆Hrxn

Hin =187347590 J/hr

Table ()

Comp

a

b

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

500

28.16

375

9084790704

O2

175430

12281

113.92

34795930

500

7.04

375

91861255200

N2

61.2899

80925

248

1.02*108

500

69.4

375

2.66659*1012

Hout = 337225662 J/hr

Table ()

Comp

a

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

500

8.45

575

4179993071

O2

175430

12281

113.92

34795930

500

2.11

575

42216162073

N2

61.2899

80925

248

1.02*108

500

69.4

575

4.08877*1012

SO3

258090

-

-

258090

500

24.64

575

3656619120

Heat evolved = 149878072 J/hr

Heat exchanger

T in =600 0C

T out =450 0C

Heat evolved = h in - h out

H in =337225662 J/hr

Table ()

Comp

a

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860445.8

525

8.45

575

4179993071

O2

175430

12281

113.92

38022155

525

2.11

575

42216162073

N2

61.2899

80925

248

1.11*108

525

69.4

575

4.08877*1012

SO3

258090

-

-

258090

525

24.64

575

3656619120

Hout = 241376427 J/hr

Table ()

Comp

a

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

525

8.45

425

3090075827

O2

175430

12281

113.92

34795930

525

2.11

425

34096367496

N2

61.2899

80925

248

1.02*108

525

69.4

425

3.26925*1012

SO3

258090

-

-

258090

525

24.64

425

2702718480

Heat evolved = -95849235 J/hr

Bed (2)

T in =4500 C

T out =6000 C

Heat of reaction (∆Hrxn) = -100 KJ/mol

Heat evolved = h in - h out + ∆Hrxn

H in = 241376427 J/hr

Table ()

Comp

a

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

525

8.45

425

3090075827

O2

175430

12281

113.92

34795930

525

2.11

425

34096367496

N2

61.2899

80925

248

1.02*108

525

69.4

425

3.26925*1012

SO3

258090

-

-

258090

525

24.64

425

2702718480

Hout = 82174153.24 J/hr

Table ()

Comp

A

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

525

26.72

575

9771222022

O2

175430

12281

113.92

34795930

525

1.62

575

26178253718

N2

61.2899

80925

248

1.02*108

525

69.4

575

3.26925*1012

SO3

258090

-

-

258090

525

26.72

575

2930870040

Heat evolved = 159202273.8 J/hr

Heat exchanger

T in =600 0C

T out =450 0C

Heat evolved = h in - h out

H in = 82174153.24 J/hr

Table ()

Comp

A

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860445.8

525

26.72

575

9771222022

O2

175430

12281

113.92

38022155

525

1.62

575

26178253718

N2

61.2899

80925

248

1.11*108

525

69.4

575

3.26925*1012

SO3

258090

-

-

258090

525

26.72

575

2930870040

Hout = 72706261.8 J/hr

Table ()

Comp

A

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

525

26.72

425

3090075827

O2

175430

12281

113.92

34795930

525

1.62

425

34096367496

N2

61.2899

80925

248

1.02*108

525

69.4

425

3.26925*1012

SO3

258090

-

-

258090

525

26.72

425

2702718480

Heat evolved = -9467891.3 J/hr

Bed (3)

T in =4500 C

T out =6000 C

Heat of reaction (∆Hrxn) = -100 KJ/mol

Heat evolved = h in - h out + ∆Hrxn

H in = 72706261.8 J/hr

Table ()

Comp

a

B

c

CP

Temperature

M

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

525

26.72

425

3090075827

O2

175430

12281

113.92

34795930

525

1.62

425

34096367496

N2

61.2899

80925

248

1.02*108

525

69.4

425

3.26925*1012

SO3

258090

-

-

258090

525

26.72

425

2702718480

Hout = 26871782.5 J/hr

Table ()

Comp

A

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

525

0.314

575

155353481.5

O2

175430

12281

113.92

34795930

525

0.0768

575

1679058365

N2

61.2899

80925

248

1.02*108

525

69.4

575

4.4231*1012

SO3

258090

-

-

258090

525

1.36

575

201826380

Heat evolved = 45834479.3 J/hr

Heat exchanger

T in =600 0C

T out =450 0C

Heat evolved = h in - h out

H in = 26871782.5 J/hr

Table ()

Comp

A

B

c

CP

Temperature

m

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860445.8

525

0.314

575

155353481.5

O2

175430

12281

113.92

38022155

525

0.0768

575

1679058365

N2

61.2899

80925

248

1.11*108

525

69.4

575

4.4231*1012

SO3

258090

-

-

258090

525

1.36

575

201826380

Hout = 15806930.88 J/hr

Table ()

Comp

A

B

c

CP

Temperature

M

(Tin-25)

m*cp* (T-25)

SO2

857430

5.7443

-

860302.2

525

0.314

425

114826486.3

O2

175430

12281

113.92

34795930

525

0.0768

425

1241043139

N2

61.2899

80925

248

1.02*108

525

69.4

425

3.26925*1012

SO3

258090

-

-

258090

525

1.36

425

149176020

Heat evolved = -11064851.62 J/hr

CHAPTER SIX

PLANT LOCATION

Plant Location

The geographic location of the plant can have a strong influence on the success of an industrial venture. Considerable care must be exercised primarily. The plant should be located where the minimum cost of production and distribution can be obtained, but other factor such as room for expansion and safe living condition for plant operation as well as the surrounding community, are also important.

There are many possible locations in Jordan for sulfuric acid production plant. A comparison was made between these locations based on the factors that should be considered in the plant site selection, which can effect the ultimate success of the over all operation.

6.1 Factor Affecting Plant Location Selection

A general consensus as to the plant location should be obtained before a design project reaches the detailed estimate design. The choice of the final site should be based first on a complete survey of the advantages and disadvantages of various geographic areas and ultimately the advantages and disadvantages of available real estate.

The following factors should be considered in selecting a plant site:

â- Availability of Raw Material

The source of raw materials is one of the most important factors influencing the selection of the plant site. This is particularly true if large volumes of raw materials are consumed, because location near the source of raw materials permits considerable reduction in transportation and storage charges. Attention should be given to the purchased price of the raw materials, distance from the source of supply, freight or transportation expenses, availability and reliability of supply, purity of the raw materials , and storage requirements.

â- Markets

The location of market or intermediate distribution centers effect the cost of product distribution and the time required for shipping. Markets are an important considerable factor in the selection of a plant site, because the buyer usually finds it advantageous to purchase from nearby sources.

â- Transportation Facilities

The kind and amount of product and raw materials determine the most suitable type of transportation facilities. In any case, careful attention should be given to local freight rates and existing railroad lines.

â- Energy Availability

Availability of power and steam requirements are high in most industrial plants, and fuel is ordinarily required to supply these utilities. Consequently, power and fuel can be combined as one major factor in the choice of a plant site.

â- Climate

If the plant is located in a cold climate, costs maybe increased by the necessity for constriction of productive shelters around the process equipment, and special cooling towers or air conditioning equipment maybe required if the prevailing temperatures are high.

Excessive humidity or extremes of hot or cold weather can have a serious effect on the economic operation of the plant. These factors should be examined when a plant site is selected.

â- Waste Disposal

Many legal restrictions have been placed in the methods of disposing of waste materials from the process industries. The site selection for a plant should have adequate capacity and facilities for correct waste disposal.

â- Water Supply

Industrial processes use large quantities of water for cooling, washing, steam generation, and as a raw material. The plant must be located where dependable supply of water is available, such as rivers, seas, lakes, and wells.

â- Taxation and Legal Restrictions

State and local tax rates on property income, unemployment insurance, and similar items vary from one location to another. Similarly, local regulations or zoning, building codes, nuisance aspects, and transportation facilities can have a major influence on the final choice of a plant site.

â-Site Characteristics

The characteristics of the land at a proposed plant site should be examined carefully. The topograph of the tract of land and soil structure must be considered, since either or both may have a pronounced effect on construction costs. The cost of the land is important as well as local building cost and living conditions. Future changes may make it desirable or necessary to expand the plant facilities. Therefore, even though no immediate expansion is planned, new plant should be constructed at a place where additional space is available.

â- Community Factors

Includes schools, hospitals, housing, restaurant, and transportation.

There are many possible plant location in Jordan for sulfuric acid production plant, comparison was made between these location based on the previous factors that should be considered in the plant site selection, which can affect the ultimate success of the over all operation. The following table summarized this comparison.

Aqaba

Al-Rsayfeh

Al-Hasa

Eshidiya

Location

6

3

8

9

Raw Material

9

4

7

7

Markets

8

9

6

6

Energy availability

8

4

7

7

Climate

10

6

8

8

Transportation

9

5

7

7

Water supply

7

4

8

9

Waste disposal

9

8

6

6

Labor supply

4

8

6

6

Taxation and legal restrictions

9

8

7

4

Site characteristics

9

6

6

7

Community factors

88

65

76

76

Total (110 )

Table (6.1): Plant Location of Sulfuric Acid in Jordan

From this table the location for sulfuric acid plant is in Aqaba city.

*Appendix (A-1):

S + O2 SO2

SO2 + 0.5 O2 SO3

SO3 +H2O H2SO4

Balance on the all equation:

We want to produce 1ton/day =1000Kg/day = 41.6 Kg/hr.

(100Kg/yr) / 98 (Kg/Kmole) =0.43 Kmole /yr.

For purity 98% mole of H2SO4 =0.43 Kmole /yr.

# Of moles of H2SO4 = # of moles SO3 ….(Completely conversion in absorption)

……Ref[2]

# Of moles of H2SO4 = 0.98 # of moles SO2 …..(Conversion in converter 0.98)

……..Ref[2]

# Of moles of SO2 = # moles of S……… (Completely conversion in Burner)

……..Ref[2]

# of moles of O2 = 1.5* moles of S=O.632 Kmole .(excess O2) ……Ref[2]

Mass of S =0.43*32Kg/Kmole=13.76 Kg/hr

Mass of SO3 = 0.43 *80Kg/Kmole= 34.4Kg/hr

Mass of SO2 = (0.43/0.98)*64Kg/Kmole=28.08Kg/hr

*Material balance on H2SO4 plant (A-2):

Assumption:

Steady state.

H2SO4 produce = 1ton/day (Basis).

Concentrated acid purity is 98%.

All heat capacity are constant with temperature.

*Table (A.1): molecular weight for component in the equation of H2SO4 formation1:

component

M.W(Kg/KMole)

H2SO4

98

S03

80

S02

64

S

32

Air

29

H2O

18

Note:

All mass flow rates in (Kg/yr).

All molar rates in (Kmole/yr).

All heat capacities are from 4

% of H2SO4 produce is 98%.

Use excess amount of air.

*Drier:

O2 need=0.66 mol/hr=21.12Kg/hr.

Dry air need = (O2need*1.5)/0.21=3.14Kmole/hr=91.14Kg/hr.

(M3=91.14 Kg/hr)

Air in at T=26 And relative humidity =0.7 then find H=0.014KgH2O/Kgdry air …….[Ref 5]

Wet air (M1=92.33Kg/hr).

From balance on H2SO4 and H2O Find :

(M2=40.2Kg/hr).

(M4=41.5Kg/hr).

*Burner:

(M3=91.14 Kg/hr).

Mass of S =0.43*32Kg/Kmole=( 3. 76 Kg/hr=M5).

M6=M3+M5=94.9Kg/hr.

Where:

M3 (O2+N2).

M5(S).

M6(SO2+O2+N2)

*Converter:

M6(O2,SO2,N2)

Amount of O2=0.22 Kmole/hr=7.04Kg/hr.

Amount of SO2=0.44Kmole/hr=28.16Kg/hr.

Amount ofN2=2.48Kmole/hr=69.44Kg/hr.

(M6=104.58Kg/hr)

M7(O2,SO2,SO3,N2)

Amount of SO3=0.308Kmole/hr.=24.64Kg/hr.

Amount of O2=0.066 Kmole/hr=2.11Kg/hr.

Amount of SO2=0.132Kmole/hr=8.45Kg/hr.

Amount ofN2=2.48Kmole/hr=69.44Kg/hr.

(M7=104.64)

M8(O2,SO2,SO3,N2)

Amount of SO3=0.334Kmole/hr.=26.72Kg/hr.

Amount of O2=0.053Kmole/hr=1.69Kg/hr.

Amount of SO2=0.106Kmole/hr=6.784Kg/hr.

Amount ofN2=2.48Kmole/hr=69.44Kg/hr.

(M8=104.63)

M9(O2,SO2,SO3,N2)=0.05*M8

Amount of SO3=0.017Kmole/hr.=1.36Kg/hr.

Amount of O2=0.0024Kmole/hr=0.0768Kg/hr.

Amount of SO2=0.0049Kmole/hr=0.3136Kg/hr.

Amount ofN2=0.124Kmole/hr=3.47Kg/hr.

(M9=5.22Kg/hr)

M11 (O2,SO2,SO3,N2)= 0.95*M8=99.37Kg/hr.

Amount of SO3=0.323Kmole/hr.=25.84Kg/hr.

Amount of O2=0.048Kmole/hr=1.54Kg/hr.

Amount of SO2=0.095Kmole/hr=6.08Kg/hr.

Amount ofN2=2.36Kmole/hr=65.97Kg/hr.

(M11=99.34)

M10(O2,SO2,SO3,N2)

Amount of SO3=0.017Kmole/hr.=1.36Kg/hr.

Amount of O2=0.0024Kmole/hr=0.0768Kg/hr.

Amount of SO2=0.0049Kmole/hr=0.3136Kg/hr.

Amount ofN2=0.124Kmole/hr=3.47Kg/hr.

(M10=5.22Kg/hr)

*Internal absorption column:

M11 (O2, SO2, SO3, N2) = 0.95*M8=99.37Kg/hr.

Amount of SO3=0.323Kmole/hr.=25.84Kg/hr.

Amount of O2=0.048Kmole/hr=1.54Kg/hr.

Amount of SO2=0.095Kmole/hr=6.08Kg/hr.

Amount ofN2=2.36Kmole/hr=65.97Kg/hr.

(M11=99.34Kg/hr).

M12 (H2SO4, H2O), (0.95%).

Amount of H2O Need =0.323Kmole/hr=5.81Kg/hr.

Amount of H2SO4 Need =6.137Kmole/hr=601.43Kg/hr.

(M11=607.24Kg/hr).

M13 (O2, SO2, N2,H2SO4)

Amount of O2=0.048Kmole/hr=1.54Kg/hr.

Amount of SO2=0.095Kmole/hr=6.08Kg/hr.

Amount ofN2=2.36Kmole/hr=65.97Kg/hr.

Amount ofH2SO4=9.17Kmole/hr=892.45Kg/hr

(M13=966.6Kg/hr).

*External absorption column:

M10(O2,SO2,SO3,N2)

Amount of SO3=0.017Kmole/hr.=1.36Kg/hr.

Amount of O2=0.0024Kmole/hr=0.0768Kg/hr.

Amount of SO2=0.0049Kmole/hr=0.3136Kg/hr.

Amount ofN2=0.124Kmole/hr=3.47Kg/hr.

(M10=5.22Kg/hr).

M14 (H2SO4, H2O), (0.95%).

Amount of H2O Need =0.017Kmole/hr=0.306Kg/hr.

Amount of H2SO4 Need =0.33Kmole/hr=32.66Kg/hr.

(M11=32.96Kg/hr).

M15 (O2, SO2, N2,H2SO4)

Amount of O2=0.0024Kmole/hr=1.54Kg/hr.

Amount of SO2=0.0049Kmole/hr=6.08Kg/hr.

Amount ofN2=2.36Kmole/hr=3.47Kg/hr.

Amount ofH2SO4=0.35Kmole/hr=54.0Kg/hr

(M11=58.18Kg/hr).


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