Mini Dp Batch Production of Amino Acid

8/10/2019 Mini Dp Batch Production of Amino Acid

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PRODUCTION OF AMINO ACID

Market demand (tons/year)

L-aspartic acid =10 000 tons/year

= 10 000 000

L-phenylalanine = 12 650 tons/year

= 12 650 000

All the stream having scale down at 0.5.



Stream tables for Aspartic Acid

Name (Stream) 1 2 3 4

VapFrac 0.00 0.00 0.00 0.00

T [oC] 30.0 30.0 30.0 30.0

P [kPa] 101.325 101.325 101.325 101.325

Flowrate/Composition kg/batch kg/batch kg/batch kg/batch

Nutrient Media 22.5 22.5 87500 87500

Biomass 2.5 2.5 0 0

Eluting Water 0 0 0 0

L-aspartic acid 0 0 0 0

Total Mass Flow

[kg/batch] 25.0 25.0 87500 87500

Volume Flow

[m3 /batch] 0.25 0.25 87.48 87.48


VapFrac 0.00 0.00 0.00 0.00

T [oC] 30.0 30.0 30.0 30.0

P [kPa] 101.325 101.325 101.325 101.325


Nutrient Media 69440 0 69440 69440

Biomass 8750 8750 0 0



Total Mass Flow

[kg/batch] 87500 8750 78750 78750

Volume Flow [m3 /hr] 87.5 - 87.5 87.5




VapFrac 0.00 0.00 0.00 0.00

T [oC] 70.0 30.0 70.0 70.0

P [kPa] 101.325 101.325 101.325 101.325


Nutrient Media 0 69440 0 0

Biomass 0 0 0 0

Eluting Water 87500 0 87500 136610


Total Mass Flow

[kg/batch] 87500 96440 96810 155230

Volume Flow [m /hr] 87.5 87.5 87.5 -


VapFrac 1.00 0.00 0.00 0.00

T [oC] 100.0 25.0 100.0 100.0

P [kPa] 101.325 101.325 101.325 101.325



Biomass 0 0 0 0

Eluting Water 35300 35300 104400 104400


Total Mass Flow

[kg/batch] 35300 35300 123020 123020

Volume Flow [m3 /hr] - - - -




VapFrac 0.00 0.00 0.00 0.00

T [oC] 100.0 100.0 100.0 100.0

P [kPa] 202.650 101.325 101.325 101.325



Biomass 0 0 0 0

Eluting Water 104400 52200 3090 49110

L-aspartic acid

L-aspartic acid (solid)

18620

0

9310

9310

0

9310

9310

0

Total Mass Flow

[kg/batch] 123020 70820 12400 58420

Volume Flow [m /hr] - - - -



Stream tables for Phenylalanine


VapFrac 0.00 0.00 0.00 0.00

T [oC] 30.0 30.0 30.0 30.0

P [kPa] 101.325 101.325 101.325 101.325


Nutrient Media 22.5 22.5 87500 87500

Biomass 2.5 2.5 0 0


L-phenylalanine 0 0 0 0

Total Mass Flow

[kg/batch] 25.0 25.0 87500 87500

Volume Flow

[m3 /batch] 0.25 0.25 87.48 87.48




VapFrac 0.00 0.00 0.00 0.00

T [oC] 30.0 30.0 30.0 30.0

P [kPa] 101.325 101.325 101.325 101.325


Nutrient Media 76851 0 76851 76851

Biomass 8750 8750 0 0



Total Mass Flow

[kg/batch] 87500 8750 78750 78750

Volume Flow [m /hr] 87.5 - 87.5 87.5


VapFrac 0.00 0.00 0.00 0.00

T [oC] 70.0 30.0 70.0 70.0

P [kPa] 101.325 101.325 101.325 101.325



Biomass 0 0 0 0

Eluting Water 34500 0 34500 51450


Total Mass Flow

[kg/batch] 34500 76851 36400 55300

Volume Flow [m /hr] 87.5 87.5 87.5 -




VapFrac 1.00 0.00 0.00 0.00

T [oC] 100.0 25.0 100.0 100.0

P [kPa] 101.325 101.325 101.325 101.325



Biomass 0 0 0 0

Eluting Water 33850 33850 39300 39300


Total Mass Flow

[kg/batch] 33850 33850 43300 43300

Volume Flow [m /hr] - - - -


VapFrac 0.00 0.00 0.00 0.00

T [oC] 100.0 100.0 100.0 100.0

P [kPa] 202.650 101.325 101.325 101.325



Biomass 0 0 0 0

Eluting Water 39300 19650 2700 16950

L-phenylalanine

L-phenylalanine

(solid)

4000

0

2000

1900

50

1900

1950

0

Total Mass Flow

[kg/batch] 43300 23500 4650 18900

Volume Flow [m3 /hr] - - - -



L-aspartic acid L-phenylalanine

Market Demand (kg/y) 1.0×107 1.256×107

Amount Produced in Process (kg/y) 2.5×105 3.14×105

Concentration of product (kg/m3) 106.4 21.7

Total Volume for Year (m3 /y) 2349 14470

Time required per batch (h/batch) 35 65Required Number of Batches(batches/y)

27 166

ENERGY BALANCE

Assumption:

Kinetic energy and potential energy is negligible

Workshaft,Ws is negligible

No heat gain or lost to the surrounding

Specific heat capacity,Cp water is 4.18kJ/kg.0 C

Specific heat capacity Cp for nutrient media 0.9cal/g.0C

Cp for L-Aspartic acid

T(K) Cp(cal/0C.mol)

300 37.28

303 X

310 38.33

By interpolation

-

X = 37.6 cal/0C.mol = Cp of L-Aspartic acid

Energy balance at fermentor,R-501

Stream 2

Stream 4

FERMENTOR,R-501

Stream 11

Stream 13



Component : L-aspartric acid

For inlet reactor

Stream 4

Nutrient media

Flowrate = 87500kg/batch

87500

÷ 35

= 2500 kg/hr

= 2.5x10 6 g/hr

Specific heat capacity

0.9

x

= 3.766 J/g.0 C

Qin(nutrient media)=ṁCp ΔT

= (2.5x10 6 g/hr)( 3.766 J/g.0C)(300C)

= 282450000J/hr

= 282450kJ/hr

So that, energy in

Qin = 282450 kJ/hr

For outlet reactor

At stream 13

Component : L-aspartic acid

Nutrient media

69440

÷ 35

= 1984 kg/hr

= 1.984x10 6 g/hr

Qout(nutrient media)=ṁCp ΔT

= (1.984x10 6 g/hr)( 3.766 J/g.0C)(300C)

= 224152320/hr

= 22452.3 kJ/hr



For L-aspartic acid

Specific heat capacity for L-aspartic acid = 37.6cal/ 0C.mol

37.6

x

= 157.32 J/mol 0C

157.32

÷133.11

= 1.182 J/g.0C

9310

÷ 35

= 266 kg/hr

= 2.66x105 g/hr

Q = ṁCp ΔT

= (2.66x105

g/hr)(1.182 J/g.0

C)(300

C)

= 9432360J/hr

= 9432.4 kJ/hr

Qtotal = 22452.3 kJ/hr + 9432.4 kJ/hr

=233584 kJ/hr

Q= Qin - Qout

=282450 kJ/hr- 233584 kJ/hr

=48865 kJ/hr

So net energy by L-aspartic acid at fermentor is

Q = 48865 kJ/hr



Component: L-phenylalanine

For inlet reactor

Stream 4

Nutrient media


87500

÷ 65

= 1346 kg/hr

= 1.346x106 g/hr


0.9

x

= 3.766 J/g.0 C


= (1.346x103 g/hr)( 3.766 J/g.0C)(300C)

=151393200 J/hr

=151393 kJ/hr

So that, energy in

Qin = 151393 kJ/hr

Outlet reactor

At stream 13

Component: L-phenylalanine


1899

÷ 65

= 29.22 kg/hr

= 29.22x103g/hr

Specific heat capacity = 203.01J/mol.K

÷165.19

= 1.23J/g. K

Q = ṁCp ΔT

= (29.22x103g/hr)(1.23J/g. K)(300C)



= 1078218J/hr

= 1078.22kJ/hr

Nutrient media


76851

÷ 65

= 1182 kg/hr

= 1182x103g/hr


0.9

x

= 3.766 J/g.0 C


= (1182x103g/hr)( 3.766 J/g.0C)(300C)

=1335 x105J/hr

=133542kJ/hr

So that,

Qout = 1078.22 kJ/hr +133542 kJ/hr

= 134620 kJ/hr

Therefore at fermentor,the energy is

Q(fermentor)= Qin – Qout

=151393 kJ/hr -134620kJ/hr

=16773kJ/hr

So net energy by L-Phenylalanine acid at fermentor is

Q=16773kJ/hr



Energy balance at ion exchange column,T-501

stream 16 stream 19

stream 17 stream 18


For inlet ion exchange column

Stream 16

Aspartic acid


9310

÷ 35

= 266 kg/hr

= 266x10 3 g/hr

Q=ṁCp ΔT

= ṁCp(T19-T16)

= (266x10 3 g/hr)( 1.182 J/g.0C)(700C-300C)

=12576000J/hr

= 12576kJ/hr

Nutrient media


69440

÷ 35

= 1984 kg/hr

= 1984x103 g/hr

Q = ṁCp(T19-T16)

= (1984x103 g/hr)( 3.766 J/g.0C)(700C-300C)

=298870000J/hr

ION

EXCHANG

E

COLUMN

T-501



=298870kJ/hr

So that,

Q= 12576kJ/hr +298870 kJ/hr

=311446 kJ/hr

At stream 17

Aspartic acid inlet

Component: Eluting water


175000

÷ 35

= 5000 kg/hr

Q= ṁCp ΔT

= ṁCp(T18-T17)

= (5000 kg/hr)( 4.18kJ/kg.0C)(300C-700C)

= - 836000kJ/hr

So that,

Qin =311446 kJ/hr +(- 836000kJ kJ/hr)

=-524554kJ/hr

For outlet ion exchange column

At stream 18

Component : L-aspartic acid

Nutrient media

69440

÷ 35

= 1984 kg/hr

= 1.984x10 6 g/hr


= ṁCp(T18-T17)

= (1.984x10 6 g/hr)( 3.766 J/g.0C)(300C-700C)

= -298870000J/hr

= -298870 kJ/hr

At stream 19



Component:L-aspartic acid

Flowrate=9310 kg/batch

9310

÷ 35

= 266 kg/hr

= 2.66x105 g/hr

Q = ṁCp ΔT

= ṁCp(T19-T16)

= (2.66x105 g/hr)(1.182 J/g.0C)(700C -300C)

=12576000J/hr

= 12576kJ/hr

Eluting water

87500

÷ 35

= 2500kg/hr

Q = ṁCp ΔT

= ṁCp(T19-T16)

= (2500kg/hr)(4.18kJ/g.0C)(700C -300C)

=418000kJ/hr

Q(out)=12576kJ/hr + 418000kJ/hr

=430576kJ/hr

Q(outlet total) = Q(outlet stream 18) + Q(outlet stream 19)

= -298870kJ/hr + 430576kJ/hr

= 131706 kJ/hr

Q= Qin – Qout

=-524554kJ/hr- 131706kJ/hr

=-656260 kJ/hr

So net energy by L-aspartic acid at ion exchange column is

Q = -656260 kJ/hr



Energy balance for component of L-phenylalanine at T-501

Component : L- phenylalanine

For inlet ion exchange column

Stream 16

L-phenylalanine


1899

÷ 65

= 29 kg/hr

= 29x103 g/hr

Q=ṁCp ΔT

= ṁCp(T19-T16)

= (29x103g/hr)( 1.23 J/g.0C)(700C-300C)

=1427000J/hr

= 1427kJ/hr

Nutrient media


76851

÷ 65

= 1182 kg/hr

= 1182x103 g/hr

Q = ṁCp(T19-T16)

= (1182x103 g/hr)( 3.766 J/g.0C)(700C-300C)

=178056000J/hr

=178056kJ/hr

So that,

Q= 1427kJ/hr +178056 kJ/hr

=179483 kJ/hr

At stream 17

L-phenylalanine acid inlet

Component: Eluting water




34500

÷ 65

= 531kg/hr

Q= ṁCp ΔT

= ṁCp(T18-T17)

= (531 kg/hr)( 4.18kJ/kg.0C)(300C-700C)

= - 88783kJ/hr

So that,

Qin = 179483kJ/hr +(- 88783kJ/hr)

=90700kJ/hr

For outlet ion exchange column

At stream 18

Component : L-phenylalanine

Nutrient media

7685

÷ 65

= 118 kg/hr

= 118x103 g/hr


= ṁCp(T18-T17)

= (118x103g/hr)( 3.766 J/g.0C)(300C-700C)

= -17776000J/hr

= -17776kJ/hr

At stream 19

Component:L-phenylalanine


1900

÷ 65

= 29kg/hr

= 29x103 g/hr

Q = ṁCp ΔT

= ṁCp(T19-T16)

= (29x103g/hr)(1.23 J/g.0C)(700C -300C)



=1427000J/hr

= 1427kJ/hr

Eluting water

Flowrate=34500kg/batch

34500

÷ 65

= 531kg/hr

Q = ṁCp ΔT

= ṁCp(T19-T16)

= (531kg/hr)(4.18kJ/g.0C)(700C -300C)

=88783kJ/hr

Q(out)= 1427 kJ/hr + 88783kJ/hr

=90210kJ/hr

Q(outlet total) = Q(outlet stream 18) + Q(outlet stream 19)

= -17776kJ/hr + 90210kJ/hr

=72434 kJ/hr

Q= Qin – Qout

= 90700kJ/hr- 72434kJ/hr

=18266kJ/hr

So net energy by L-phenylalanine acid at ion exchange column is

Q = 18266 kJ/hr



Energy balance for crystallizer,CR-501

stream 21

stream 20 stream 23

stream 25 stream 26


For inlet crystallizer

At stream 20

L-Aspartic acid


18620

÷ 35

= 532 kg/hr

= 532x103 g/hr

Q=ṁCp ΔT

= (532x103 g/hr)( 1.182 J/g.0C)(300C)

=18864720J/hr

= 18864kJ/hr

Eluting water


136610

÷ 35

=3903.14kg/hr

Q = ṁCp ΔT

= (3903.14kg/hr)(4.18kJ/g.0C)(300C)

=489454kJ/hr

Q(inlet stream 20) =18864kJ/hr+489454kJ/hr

=508318 kJ/hr

CRYSTALLIZER,

CR-501



At stream 25

L-aspartic acid


18620

÷ 35

= 532 kg/hr

= 532x103 g/hr

Q=ṁCp ΔT

= (532x103 g/hr)( 1.182 J/g.0C)(300C)

=18864720J/hr

= 18864kJ/hr

Eluting water


104400

÷ 35

=2983kg/hr

Q = ṁCp ΔT

= (2983kg/hr)(4.18kJ/g.0C)(300C)

=374068kJ/hr

Q(inlet stream 25)=18864kJ/hr+374068kJ/hr

=392932 kJ/hr

Q(total inlet) =Q(inlet stream 20) + Q(inlet stream 25)

= 508318 kJ/hr +392932 kJ/hr

=901250kJ/hr

For outlet crystallizer

At stream 21

Component:L-aspartic acid

Eluting water


35300

÷ 35

=1009kg/hr



Q = ṁCp ΔT

= (1009kg/hr)(4.18kJ/g.0C)(300C)

=126529kJ/hr

At stream 23 outlet


18620

÷ 35

= 532 kg/hr

= 532x103 g/hr

Q=ṁCp ΔT

= (532x103 g/hr)( 1.182 J/g.0C)(300C)

=18864720J/hr

= 18864kJ/hr

Eluting water


104400

÷ 35

=2983kg/hr

Q = ṁCp ΔT

= (2983kg/hr)(4.18kJ/g.0C)(300C)

=374068kJ/hr

Q(outlet stream 23)=18864kJ/hr+374068kJ/hr

=392932 kJ/hr

At stream 26 outlet

Aspartic acid


9310

÷ 35

= 266 kg/hr

= 266x103 g/hr

Q=ṁCp ΔT

= (266x103 g/hr)( 1.182 J/g.0C)(300C)

=9432360J/hr

= 9432kJ/hr



Eluting water


52200

÷ 35

=1491kg/hr

Q = ṁCp ΔT

= (1491kg/hr)(4.18kJ/g.0C)(300C)

=177942kJ/hr

Q(outlet stream 26)=9432kJ/hr+177942kJ/hr

=187374kJ/hr

So that,total energy outlet at crystallizer by aspartic acid

Q(outlet) = Q(outlet stream 21) +Q(outlet stream 23) +Q(outlet stream 26)

=126529kJ/hr +392932 kJ/hr +187374kJ/hr

=706835kJ/hr

Q= Qin – Qout

= 901250kJ/hr -706835kJ/hr

=194415kJ/hr

So net energy by L-aspartic acid at crystallizer is

Q = 194415kJ/hr



Component : L-phenylalanine acid

For inlet crystallizer

At stream

Phenylalanine acid


3850

÷ 65

= 59.23 kg/hr

= 59.23x103 g/hr

Q=ṁCp ΔT

= (59.23x103 g/hr)( 1.23J/g.0C)(300C)

=2185587J/hr

= 2186kJ/hr

Eluting water


51450

÷ 65

=791.54kg/hr

Q = ṁCp ΔT

= (791.54kg/hr)(4.18kJ/g.0C)(300C)

=99259kJ/hr

Q(inlet stream 20) =2186kJ/hr+99259kJ/hr

=101445kJ/hr

At stream 25 inlet

L-phenylalanine acid


4000

÷ 65

= 61.54 kg/hr

=61.5x103 g/hr

Q=ṁCp ΔT

= (61.5x103 g/hr)( 1.23J/g.0C)(300C)

=2269350J/hr

=2269kJ/hr



Eluting water


39300

÷ 65

=604.61kg/hr

Q = ṁCp ΔT

= (604.61kg/hr)(4.18kJ/g.0C)(300C)

=75819kJ/hr

Q(inlet stream 25)=2269kJ/hr+75819kJ/hr

=78088kJ/hr

Q(total inlet) =Q(inlet stream 20) + Q(inlet stream 25)

= 101445kJ/hr +78088kJ/hr

= 179533kJ/hr

For outlet crystallizer

At stream 21

Component:L-phenylalanine acid

Eluting water


33850

÷ 65

=521kg/hr

Q = ṁCp ΔT

= (521kg/hr)(4.18kJ/g.0C)(300C)

=65333kJ/hr

At stream 23 outlet

L-phenylalanine acid


4000

÷ 65

= 61.54 kg/hr

=61.5x103 g/hr

Q=ṁCp ΔT

= (61.5x103 g/hr)( 1.23J/g.0C)(300C)





So that,total energy outlet at crystallizer by aspartic acid

Q(outlet) = Q(outlet stream 21) +Q(outlet stream 23) +Q(outlet stream 26)

=65333kJ/hr +78088 kJ/hr +380173kJ/hr

=523594kJ/hr

Q= Qin – Qout

= 179533kJ/hr -523594kJ/hr

=-344061kJ/hr

So net energy by L-phenylalanine at ion exchange column is

Summary of Net Energy Balance on Major Equipment

L-aspartic Acid

Equipment Sub-equipments

Energy In(kJ/hr)

Energy out(kJ/hr)

∆H (kJ/hr)

Fermentor R-501 282450 233584 48865

Ion Exchange

Column T-501

-524554 131706 -656260

Crystalizer CR-501 901250 706835 194415

L-phenylalanine

Equipment Sub-equipments

Energy In(kJ/hr)

Energy out(kJ/hr)

∆H (kJ/hr)

Fermentor R-501 151393 134620 16773

Ion ExchangeColumn T-501

90700 72434 18266

Crystalizer CR-501 179533 523594 -344061

Q = -344061kJ/hr



HEAT EXCHANGER NETWORK

L-aspartic Acid

STREAM 21-22

ṁCp = 4216 kJ/h.oC

T(S22) - T(S21) = 100 – 25

= 75oC

Q = ṁCp ΔT

= 4216(75)

= 87.83 kW

L-phenylalanine

STREAM 21-22

ṁCp = 2177 kJ/h.oC

T(S22) - T(S21) = 100 – 25

= 75oC

Q = ṁCp ΔT

= 2177(75)

= 45.35 kW

Cascade diagram for L-aspartic Acid

C.U. = 87.83 kW

Cascade diagram for L-phenylalanine

C.U. = 45.35 kW

Minimum no. of Heat Exchanger = 1

L-aspartic Acid L-phenylalanine

Q = 87.83

kW

Q = 45.35

kW

C.U. =

45.35 kW

Q = 87.83

kW

C.U. =

87.83 kW

Q = 45.35

kW



Preliminary Design

Reactor R-501 (fermentor)

Based on Table 11.17

Rule 6 : Batch reaction are conducted in stirred tank for small daily production rate or when

the reaction time are long or when same condition such as fit rate of temperature

must be programmed in some way.

Rule 11 : The effect of temperature on chemical reaction rate is to double the rate every

10oC.

Rule 12 : The rate of reaction in a heterogeneous system is more often controlled by the rate

of heat or mass transfer than by the chemical reaction kinetics.

Tower T-501 (ion-exchange column)

Based on Table 11.13

Rule 2 : For ideal mixtures, relative votality is the ratio of vapor pressure α12=

.

Rule 14 : Limit the tower height to about 53m (175ft.) max. because of wind load and

foundation consideration. An additional criterion is that L/D be less than 30

(20<L/D<30 often will require special design).

Heat Exchanger E-502

Based on table 11.11

Rule 3 : Tube side is for corrosive, fouling, scaling, and high pressure fluids.

Rule 7 : Cooling water inlet is 30oC (90oF), maximum outlet 45oC (115oF).

Vessel V-501 (Storage)

Based on table 11.7

Rule 2 : Between 3.8 and 38m3 (1 000 and 10 000gal), use horizontal tanks on concrete

supports.

Rule 7 : Capacities of storage tank are at least 1.5×the size of connecting transportation

equipment, for instance, 28.4m3 (7500gal) tanker trucks, 130m3 (34500gal) rail car

and virtually unlimited barge and tanker capacities.

Documents

Mini Dp Batch Production of Amino Acid