Refinery Planning Presentation

8/13/2019 Refinery Planning Presentation

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Refinery Modeling

Aaron Smith, Michael Frow,Joe Quddus, Donovan Howell,Thomas Reed, Clark Landrum,

Brian CliftonMay 2, 2006


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The

Big

Black

Box


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The

Big

Black

Box

DemandCrude B

Crude C

Crude A

Costs

Profit


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The

Big

Black

Box

DemandCrude B

Crude C

Crude A

Costs

Profit


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Hydrotreating

INPUT:

TemperaturePressure

H2/HC RatioSulfur %Nitrogen %

OUTPUT:

Sulfur %Nitrogen %Aromatic %

MODEL:

PBR


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http://www.osha.gov/dts/osta/otm/otm_iv/otm_iv_2fig25.gif


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A future of energy production

Hydrotreating

Removal of sulfur, nitrogen, andaromatics.

Government regulations are leading toincreased sulfur removal requirements.


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Typical ProcessingConditions

35580020000.75-2.0Heavy Gas

Oil

42570015000.7-1.5Light GasOil

3304008001.0-4.0Middle

Distillate

2902003001.0-5.0Naptha

Temperature(oC)

H2Pressure

(psia)H2/HCSpacevelocity


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Hydrotreating

Cracking is assumed to be insignificant.

Therefore, properties such as density and

molecular weight are assumed to beconstant.


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Hydrotreating

Cracking is assumed to be insignificant.

Therefore, properties such as density and

molecular weight are assumed to beconstant.


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Hydrotreating Model

For MoCo catalyst reaction rates are:

Rates= ksCs2CH2

.75

Raten= knCn1.4CH2.6 Ratear= karCarCH2

http://www.chem.wwu.edu/dept/facstaff/bussell/research/images/thio-HDS.jpg


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Delayed Coking

INPUT:

CCRPressure

OUTPUT:

Gas OilCokeGas

Naptha

MODEL:

Correlation


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Delayed Coking

Used to processbottoms from thevacuum distillate.

Breaks down thisportion into usablenapthas, gas, andgas oil.


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Delayed Coking

Coke Products

Shot Coke

Sponge Coke

Needle Coke


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Delayed Coking Model

Most important parameter is the ConradsonCarbon Residue.

Coke = 1.6 x CCR

Gas = 7.8 + .144 x CCR

Naptha = 11.29 + .343 x CCR

Gas oil = 100 Coke Gas - Naptha

This is an estimate from Gary and Handwerk


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Effect of Pressure onProduct

44.951.243.1Gas Oil Yield

1512.517.5Naptha Yield

9.99.110.4Gas Yield

30.227.229Coke

35 psig15 psigCorrelation

18.1CCR (wt%)


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Delayed Coking Model

Modified EquationsGas = (7.4 + (.1 x CCR)) + (.8 x (P-15)/20)

Naptha = (10.29 + (.2 x CCR)) + (2.5 x (P-15)/20)Coke = (1.5 x CCR) + (3 x (P-15)/20)

Gas oil = 100 Gas Naptha - Coke


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New Correlation

44.951.243.449.7Gas Oil Yield

1512.516.413.9Naptha Yield

9.99.110.09.2Gas Yield

30.227.230.227.2Coke

35 psig15 psigCorrelation(35 psig)

Correlation(15 psig)

18.1CCR (wt%)


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Catalytic

Reforming

INPUT:

TemperaturePressure

% Napthenes% Aromatics% Paraffins

OUTPUT:

HydrogenLPGReformate

MODEL:

PBR


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Catalytic Reforming


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Catalytic ReformingHydrogen Intensive Process Units

Xylenes Isomerization

Boilers


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Catalytic Reforming

Simplified reactions and equations from

Case Study 108 by Rase

( )

( )

( )

( ) napthenesofingHydrocrack

paraffinsofingHydrocrack

HnapthenesParaffins

HaromaticsNapthenes

__4

__3

2

*31

2

2

+

+


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Catalytic Reforming

( ) 543212215151515153

4 Cn

Cn

Cn

Cn

Cn

Hn

HC nn +++++

( ) 5432122215151515153

33 C

nC

nC

nC

nC

nH

nHC nn ++++

+

+

( ) 22222 HHCHC nnnn ++

( ) 2622 31 HHCHC nnnn +


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Catalytic Reforming[ ]

( )( )( )atmcatlbhr

moles

TkP

._,

3475021.23exp1 =

=

)

[ ]( )( )( )2

2._

,5960098.35expatmcatlbhr

molesT

kP =

=

)

[ ]( )( )._

,62300

97.42exp43catlbhr

moles

Tkk PP =

==

))

[ ] 33

1 ,46045

15.46exp*

atmTP

PPK

N

HAP =

==

[ ] 12 ,12.78000

exp*

=

== atm

TPP

PK

HN

PP


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Catalytic Reforming

[ ]

( )( )._

____*

2

22

catlbhr

paraffinstoconvertednapthenemoles

K

PPPkr

P

PHNP =

=

)

)

[ ]( )( )._

____33

catlbhr

inghydrocrackbyconvertedparaffinsmoles

P

Pkr PP =

=

)

)

[ ] ( )( )._____*

1

3

11catlbhr

aromaticstoconvertednapthenemoles

K

PPPkr

P

HANP =

=

)

)

[ ]( )( )._

____44

catlbhr

inghydrocrackbyconvertednapthenesmoles

P

Pkr NP =

=

)

)


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Catalytic Reforming


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Catalytic Reforming


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Xylenes

Isomerization

INPUT:

Temperature

OUTPUT:

BenzeneTolueneO-Xylene

P-XyleneEthyl-Benzene

MODEL:

Correlation


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Xylenes IsomerizationParaffins & Napthenes - Blending

Mixed Aromatics Fractionation


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Benzene & Toluene Solvent Quality


C9+ Aromatics Blending


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Xylenes IsomerizationO-Xylene Chemical Feedstock

Mixed Aromatics Blending

P-Xylene Chemical Feedstock


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Reaction driven by equilibrium

Temperature dependence of equilibriummodeled in Kirk-Othmer Encyclopedia ofChemical Technology

neEthylBenzeXylenepXyleneoXylenem


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Solvent

Extraction

INPUT:

TemperatureS/F Ratio

OUTPUT:

Lube OilAromatics

MODEL:

Correlation


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Solvent Extraction


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Solvent ExtractionParaffinic Oils - Solvent Dewaxing

Mixed Aromatics Blending


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Solvent Extraction Furfural Extraction Averaged K Values

Benzene from Cyclohexane Benzene from Iso-octane

1,6-diphenylhexane from Docosane

Temperature (R) dependence of K correlated from this

=

=N

n

nE

Extracted

0

11%F

SKE *=

( ) 371.7*0259.0522 += TETK


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Solvent Extraction Correlations developed from Institut Franais

du Ptrole data

( ) 9318.00426.0*% +

= F

SieldRaffinateY

( ) 9229.0)0073.0(*0004.0*..2

+

=

F

S

F

SGRaffinateS


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Solvent Extraction


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Solvent Extraction


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Visbreaker

INPUT:

Temperature

OUTPUT:

GasGasolineGas Oil

Residue

MODEL:

PFR


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Visbreaking


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Visbreaking Carbon chains cracking into smaller chains of varying

carbon numbers


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Visbreaking

Si-2 + O2

Si-3 + O3

Si-j

+ Oj

S2 + Oi-2

S1 + Oi-1

Si

Si forms all components with carbons less than i-1


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Visbreaking

Si is formed from all components with carbons greaterthan i+1

Si-2 + O2

Si-3 + O3

Si-j + Oj

S2 + Oi-2

S1 + Oi-1

Sn

Sn-1

Sk

Si+3

Si+2

On-i

On-1-i

Ok-i

O3

O2

Si

Si forms all components with carbons less than i-1


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Visbreaking

First order kinetics with molar concentrations

=+=

=

2

1

,

2

,

i

j

jii

n

ik

kiki KCsCsKrs +=

=

n

ij

jijji CsKro1

,

ii rs

FdzdCs 2

41=

i

i roFdz

dCo 2

41=


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Visbreaking

Rate Constant dependent on molecular weight

RTB

jiji

jieAK/

,,,

= jiji PMbPMbbB ++= 210,

[ ]( )

2

3

4

2

1

2

210,

++=

a

a

PMPM

iiji

ij

ePMaPMaaA11.35

146.9532.06E+06

-4.51.90E+08

428941.51E+12

ba


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Visbreaking

Model inputs

Temperature and mass flow rate

Model Product form

Weight percents Components are lumped into 4 categories

Gas: C1-C4

Gasoline: C5-C10 Gas Oil: C11-C21

Residue: C22-C45


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I i ti


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Isomerization

INPUT:

TemperatureH2/HC Ratio

OUTPUT:

HydrocarbonsC4-C6

MODEL:

PFR


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Isomerization


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Isomerization

Main reactants: n-Butane, n-Pentane, n-Hexane

Typically catalyzed-gas phase reaction

Low temperature favors isomer formation

Seven rate laws

Only one of n-Pentanes isomers forms

n-Butane i-Butane

n-Pentane i-Pentane

3-MP 2,2-DMB

2-Mp 2,3-DMB

n-Hex.


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Isomerization

n-Butane

n-Pentane

n-Hexane

2

4

2

4

214

H

Ciso

H

CnCn

PPK

PPKr

+=

[ ] ( )[ ]55

125.0

2

525 10000197.0 CieqCneq

CnCn CKCKt

H

CKr

+

=

==

+

=

5

1

,

5

1

,

j

jjii

j

iji CKCKr


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Isomerization

Model inputs Temperature, mass flow rate, and H2/HC ratio

Model Product form

Weight percents of the individual isomers


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Hydrocracking


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Hydrocracking

INPUT:

APIKwH2/BBL

OUTPUT:

NapthaLightHeavy

C3Upi-Butane

n-Butane

Gas Oil

MODEL:

Correlation


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Hydrocracking

Convert higher boiling point petroleum fractions

into lighter fuel products


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Hydrocracking Complementary Reactions

Cracking reactions Provides olefins for hydrogenation

R-C-C-C-R + heat R-C=C + C-R

Hydrogenation reactions

Provides heat for cracking

R-C=C + H2 R-C-C + heat


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Hydrocracking Feedstocks- Heavy distillate stocks, aromatics,

cycle oils, and coker oils

Catalysts- zeolites

Operating conditions-

500-30002000-3000Pressure (psi)

500-900750 -800Temperature (F)

0.5-100.2-1LHSV (hr-1)

1000-24001200-1600HydrogenConsumption (SCFB)

DistillateResiduum

Hydrocracking Model


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Hydrocracking Model

Development

Correlated data from Oil and GasJournal W.L. Nelson

Graphical correlated data was made

continuous for hydrogen feed rate, Kwand API of the feed

3 inputs

5 outputs


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Hydrocracking Model


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Hydrocracking Model

y = 0.84165e0.00096x

R2= 0.99872

y = 0.91507e0.00099x

R2= 0.99903

y = 1.03077e0.00102x

R2= 0.99873

y = 1.17542e0.00105x

R2= 0.99820

y = 1.35330e0.00110x

R2= 0.99840

y = 1.48461e0.00120x

R2= 0.99938

y = 1.64851e0.00129x

R2= 0.99707

y = 1.80073e0.00143x

R2= 0.98730

y = 2.20169e0.00147x

R2= 0.98763

y = 2.67927e0.00153x

R2= 0.98715

y = 3.40926e0.00157x

R2= 0.98555

0

10

20

30

40

50

60

70

80

90

100

0 500 1000 1500 2000 2500 3000

Hydrogen Rate SCFB

32.5

30

27.5

25

22.5

20

17.5

15

12.510

7.5


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Hydrocracking Model

y = 1.852E-05x4- 1.206E-03x3+ 2.920E-02x2-

2.531E-01x + 1.546E+00

R2= 9.992E-01

0

0.5

1

1.5

2

2.5

3

3.5

4

0 10 20 30 40

API of Feed

A

Constant

y = 6.024E-11x6- 6.539E-09x5+ 2.738E-

07x4- 5.600E-06x3+ 5.935E-05x2- 2.996E

04x + 1.509E-03

R2= 9.982E-01

0

0.0002

0.00040.0006

0.0008

0.001

0.0012

0.0014

0.0016

0.0018

0 10 20 30 40

API of Feed

BC

onstant


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Hydrocracking Model

Vol% of light naptha

Hydrogen Rate(SCFB) 7.5 10 12.5 15 17.5 20 22.5 25

2500 Kw=12.1 9.25 11 13 16 21 30 45 80

diff. from Kw=10.9 0.75 1 1 1.25 1.75 2.5 5 7.5

8.11% 9.09% 7.69% 7.81% 8.33% 8.33% 11.11% 9.38%

1500 Kw=12.1 3.4 4 4.8 5.8 7.3 9.1 11.25 14.25

diff. from Kw=10.9 0.35 0.45 0.5 0.55 0.7 1 1.5 1.75

10.29% 11.25% 10.42% 9.48% 9.59% 10.99% 13.33% 12.28%

500 Kw=12.1 1.4 1.55 1.7 2 2.3 2.8 3.4 4.2

diff. from Kw=10.9 0.1 0.17 0.2 0.2 0.25 0.3 0.35 0.4

7.14% 10.97% 11.76% 10.00% 10.87% 10.71% 10.29% 9.52%

API


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Hydrocracking Model

y = -0.7691x + 11.739

R2= 0.9916

0

0.5

1

1.5

2

2.5

3

3.5

4

10.5 11 11.5 12 12.5

Kw

slope


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Hydrocracking Equations

HBw AeKpvol = )00833.000833.1(% 1

)%(11.739)+K0.7691-(% 1w2 pvolpvol =

)%(0.337% 13 pvolpvol =)%(0.186% 14 pvolpvol =

)%(0.091% 15 pvolpvol +=


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Hydrocracking Model

Hydrogen

(SCFB)

15 2500 12.1 16.4 39.9

actual 15.0 40.5

20 750 10.9 3.3 11.0actual 3.5 10.0

30 1250 10.9 16.3 54.7

actual 13.0 43.0

API Kw vol% p1 vol% p2

9%

25%

7%

1%

27%

9%


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Solvent

Dewaxing


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Dewaxing

INPUT:

CompositionTemperature

OUTPUT:

WaxLube Oil

MODEL:

Correlation


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Solvent Dewaxing

Separate high pour point waxes from

lubricating oils


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Solvent Dewaxing

Feedstocks Distillate and residual stocks heavy gas oils

Solvents Ketones (MEK) and Propane

Operating conditions

Solvent to oil ratio 1:1 to 4:1

Desired pour point of product

Dewaxing Model


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Development Correlation from Energy and Fuels

Krishna et. al. 3 experimentally determined parameters

3 inputs

2 outputs

2/1)/100log(0 ACLAPCAPPT ++=

( )( ))(100

)(100%)(productPC

feedPCwtOilYield

=


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Dewaxing Model ErrorBC2 NC6 NC7 NC8 NC9 NC10

C 375-500 375-400 400-425 425-450 450-475 475-500

wax wt% 46.8 44.88 47.28 48.41 48.72 47.05

CL 26.89 24.13 25.13 27.14 29.05 31PPT act. 48 39 45 48 51 57

PPT pred. 48.0 41.0 44.0 48.9 52.8 55.9

error % 0.1% 5.0% 2.3% 1.8% 3.5% 1.9%

dewaxing model Desired PPT= 10PPT low 9.99 9.50 9.77 9.82 9.65 9.81

PPT high 10.01 10.50 10.23 10.18 10.35 10.19

wax wt% low 0.368 0.819 0.608 0.336 0.202 0.133

wax wt% high 0.369 0.931 0.643 0.352 0.220 0.139

yield low 0.5340 0.5558 0.5304 0.5176 0.5138 0.5302yield high 0.5340 0.5564 0.5306 0.5177 0.5139 0.5302

error % 0.001% 0.112% 0.036% 0.016% 0.019% 0.006%


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Alkylation


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INPUT:

Iso-butaneButylene /Propylene

Reaction time

OUTPUT:PropaneButaneAlkylate

MODEL:

Correlation


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Alkylation PFD

http://www.prod.exxonmobil.com/refiningtechnologies/pdf/AlkyforWR02.pdf

Exxon-Mobil Autorefrigeration H2SO4 alkylation


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Alkylation

*Lots of side reactions

Alk l i


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Alkylation

O

FE

SV

OIIF

)(100

)/(=

FOI )/(

=EI

=OSV)(

= volumetric isobutane/olefin ratio in feed

isobutane in reactor effluent, liquid volume %

F= Factor defined by A.V. Mrstikolefin space velocity, v/hr/v

Progress in Petroleum Technology AV Mrstik et al. ACS Publications


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Polymerization


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INPUT:

Iso-butaneButylene /Propylene

OUTPUT:GasolineDiesel

MODEL:

Correlation

PolymerizationPolymerizationPolymerizationPolymerization


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Converts Propylenes and butylenes into saturatedcarbon chains

1st used Catalytic Solid Phosphoric Acid (SPA) on

silica fell out of popularity in 1960s. Now experimenting with Zeolites.

C C

C

C + C C

C

C

C C

C

CC C

C

C

C C C + C C C C C

C

CC C

- Polymerization reaction is highly exothermic and temperature iscontrolled either by injecting cold propane quench or by

generating steam.

- Propane is also recycled to help control temperature

CO School of Mines http://jechura.com/ChEN409/11%20Alkylation.pdfhttp://www.personal.psu.edu/users/w/y/wyg100/fsc432/Lecture%2015.htm

Z litZ litZ litZ lit P l i tiP l i tiP l i tiP l i ti


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ZeoliteZeoliteZeoliteZeolite PolymerizationPolymerizationPolymerizationPolymerization Converts propylenes and butylenes into

saturated carbon chains by means ofzeolite catalysis (ZSM-5)

Z litZ litZ litZ lit P l i tiP l i tiP l i tiP l i ti


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ZeoliteZeoliteZeoliteZeolite Pol e izatioPol e izatioPol e izatioPol e izatio


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79MON

92RON

Octane

0.73SpecificGravity

[Tabak, 1986]

ZeoliteZeoliteZeoliteZeolite PolymerizationPolymerizationPolymerizationPolymerization


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ZeoliteZeoliteZeoliteZeolite PolymerizationPolymerizationPolymerizationPolymerizationCharge

17wt.% Propylene

10.7 wt.% Propane

36.1 wt.% 1-butene

27.2 wt.% isobutane

Temperature = 550K

Total Pressure =5430 kPa

Propylene partial pressure =7~3470kPa.

*Depending on desiredchain length

ZeoliteZeoliteZeoliteZeolite PolymerizationPolymerizationPolymerizationPolymerization


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ZeoliteZeoliteZeoliteZeolite PolymerizationPolymerizationPolymerizationPolymerizationCharge

17wt.% Propylene

10.7 wt.% Propane

36.1 wt.% 1-butene

27.2 wt.% isobutane

Temperature = 550K

Total Pressure =5430 kPa

Propylene partial pressure =7~3470kPa.

*Depending on desiredchain length

Polymerization

+ PBR-gas phase

Alkylation

- CSTR- liquid phaseVS


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+ PBR-gas phase

- Solid catalysis

+ Produce eitherdiesel or gasolinerange chains

- Typical octanenumber = 92(RON)

- CSTR liquid phase

+ Liquid catalysis

- Requires very vigorousagitation

- Typically .1lbmacidconsumed per gallonproduct

++Typical octane number =96(RON)

VS


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Deasphalting

INPUT MODEL:


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INPUT:

%HeaviesTemperaturePressure

OUTPUT:%HeaviesLube oil

MODEL:

Correlation

Propane Deasphalting - PFD


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Propane Deasphalting - PFD

http://www.scielo.br/scielo.php?script=sci_arttext&pid=S0104-66322000000300012&lng=pt&nrm=iso

Typical Propane Deasphalting

Propane Deasphalting


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Propane Deasphalting

Types

1. Sub Critical. (below 369K) Modeled first byRobert E. Wilson in 1936. Hildebrandsolubility parameters now used.

2. Super Critical. (above 369K) Now popular.High selectivity. No good model.

Both remove greater than 99% asphalt

Sub Critical Propane

Deasphalting


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Deasphalting

21

=

VTRH g

=

=H

=gR

Hildebrand solubility

Solubility Parameter [J/mol]

Heat of vaporization [J/mol]

Universal gas Constant [8.314J/mol/K]T = Temperature [K]V = molar volume [L/mol]

Super Critical Propane

Deasphalting


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Deasphalting

Models typically break down near the critical point. Including

Redlick-Kwong, Soave-Redlick-Kwong and Perturbed-Hard-Chain(PHC). Therefore correlations have to be used.

Typically operate atT=400KPressure=55 barRatio= 4:1 propane to oil

mixture

Pressure (bar)

Phase Equilibria in Supercritical Propane Systems for Separation of Continuous Oil Mixtures Radosz, Maciej et al. Ind. Eng. Chem. Res. 1987, 26, 731-737


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Catalytic

Cracking

INPUT: MODEL:


104/142

INPUT:

KwTemperature

OUTPUT:Gas OilGasolineLPGDry Gas

Coke

PFR

Fluidized Catalytic Cracking


105/142


Pretreated feedstock is fed intothe bottom of the riser tubewhere it meets very hotregenerated catalyst.

The feed vaporizes and iscracked as it passes up theriser. 1

http://www.uyseg.org/catalysis/petrol/petrol2.htm



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Different yields of products willoccur depending on:

Temperature

Inlet Feed Properties

Top of the riser, the catalystseparates from the mixture andis steam stripped

The final product exits the topof the reactor

2




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One product from catalyticcracking is coke or carbon thatforms on the surface of thecatalyst.

To reactivate catalyst, it mustbe regenerated.

3




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z y g

Catalysis is regenerated byentering a combustion chamberand mixed with superheated air

Energy released fromregenerating the catalysis isthen coupled with the inlet feedat the bottom of the riser

Cracking4




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A B C

DE

Ancheyta-Juarez, Jorge, Estimation of Kinetic Constants., Energy & Fuels,2000, 14, 1226-1231

y g



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A B C

DE


y g



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A B C

DE


y g


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A B C

DE

8 kinetic constants

One catalyst deactivation

Gas Oil considered as a second order reaction


g



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Assumptions

One-dimensional tubular reactor

No radial and axial dispersion

Cracking only takes place in the riser

Dispersion/Adsorption inside catalyst isnegligible

Coke deposited does not affect the fluid flow



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Change Temperature

Inlet Feed

Mass Balance:

dtdt

dCCC ii *0 +=

i

C

Li rWHSVdz

dy = )(1



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Change Temperature

Inlet Feed

Mass Balance:

dtdt

dCCC ii *0 +=

i

C

Li rWHSVdz

dy = )(1

TEMPERATURE:480, 500, 520 C



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Constant C/O Ratio of 5 Varying space velocity (WHSV)

6 48 h-1

Gas Oil Conversion ~ 70 %

Gasoline ~ 50%

LPG ~ 12 %



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6 48 h-1


Gasoline ~ 50%

LPG ~ 12 %



119/142


6 48 h-1


Gasoline ~ 50%

LPG ~ 12 %


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Blending

INPUT:

35 streams


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OUTPUT:Gasoline

RegularPremium

LPG

CokeLube Oil

WaxAsphalt

Blending


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Final products are created by blendingstreams from refinery units

35 streams from 13 units are blended

30 streams are used in gasoline

5 streams are other products

Propane gas, lube oil, asphalt, wax, andcoke

Blending Indexes


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Most properties do not blend linearly Empirical blending indexes are used to

linearize the blending behavior

=i

iimix BIxBI

icomponentoffractionvolumetheisIndexBlendingtheisWhere

ixBI

Blending Indexes( ) 25.1RVPVPBI =Reid Vapor Pressure


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=08.0

1

pp TBIPour Point

10

10

log3

log

+=vBIViscosity Index

=05.0

1

CLCL TBICloud Point

6.42

24141188.6log10

+=

F

F

TBI

Flash Point

( )[ ]APBIAP 00657.0exp124.1=Aniline Point

( )RVPVPBI =e d apo essu e

Gasoline Blending


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Specifications: Octane (normal 87, premium 91)

Reid Vapor Pressure (EPA mandated)

Maximum additive amounts Inputs:

Market conditions (Price, Demand)

Incoming streams from refinery units Objective: Maximize Profit

Gasoline Blending


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Vapor pressure blending can beimproved by using thermodynamicallybased methods

Raoult's Law

=

*

ii

PxP

Blending


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Other possible products Fuel oils

Lube oils

Diesel fuel

Blending requires data for aniline point,pour point, cloud point, flash point, anddiesel index

Refinery Planning

Addresses the planning of short-term crude oil


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Addresses the planning of short-term crude oilpurchasing and processing

Does not address risk or uncertainty

Determine purchasing schedule to meet: Specification (Octane, n-Butane, etc.)

Demand with HIGHEST profit

Decision Variables: Crude oil purchase

Processing variables Temperatures, Pressures, Blending mixtures


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Refinery Planning

Max Profit


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=

Tt Cc Tt Cctctctctctc

Tt Cctc

o ppclALcoACcpMANU ,,,,,,

Pongsakdi, Arkadej, et. al, Financial risk., Int. J. Production Economics, accepted 20 April 2005

Refinery Planning

Max Profit


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=


Tt Cctc

o pp

clALcoACcpMANU,,,,,,

Product Sales

Amount of product producedin that time period multipliedby

unit sale price of product c


Refinery Planning

Max Profit


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=


Tt Cctc

o pp


Product Sales



Crude Oil Costs

Amount of crude oil refined inthat time period multipliedby

unit purchase price of crude oil


Refinery Planning

Max Profit


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=


Tt Cctc

o pp


Product Sales



Crude Oil Costs

Amount of crude oil refined inthat time period multipliedby

unit purchase price of crude oil

Discounted Expense

Amount of product volumethat cannot satisfy demand

multipliedby discounted price



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Modeling


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A Visual Basic macro in Excel was usedto help Solver find the optimal crudeselection

Model Inputs

Inputs:

Crude A: $71 88 / barrel (Australia)


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Crude A: $71.88 / barrel (Australia)

Crude B: $72.00 / barrel (Kazakhstan) Crude C: $71.20 / barrel (Saudi Arabia)

Regular Gasoline:

$2.75 / gal ($2.12) Demand: 310,000 bbl/month

Premium Gasoline:

$3.00 / gal ($2.31)

Demand: 124,000 bbl/month

Energy Information Administration, U.S. Department of Energyhttp://www.eia.doe.gov/oil_gas/petroleum/info_glance/petroleum.html

Model Results


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Outputs: Maximum Profit: $21 per barrel

Crude Selection:

Crude A: 150,000 bbl/month Crude B: 150,000 bbl/month

Crude C: 300,000 bbl/month

Demand exactly met

Future Work


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Include storage of crude and products Include risk and uncertainty

Demand changing over time

Wider variety of products: diesel,solvents, fuel oils, lube oils, etc.

Questions?


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Refinery Planning Presentation

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