Urea.pdf

SimSci® ®

PRO/II 9.3 Urea Plant Casebook

May 2014

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Case 5: Urea Plant ABSTRACT This case book demonstrates the use of PRO/II® in the simulation of a chemicals processing plant manufacturing 1000 tons per day of urea from ammonia and carbon dioxide. Urea is widely used as a solid fertilizer, as a protein supplement for livestock, as well as a feedstock for the manufacture of plastics and adhesives. The process plant simulated here includes a reactor, an NH3 recovery distillation column, and a series of crystallizers. SIMSCISM's NRTL databank, along with urea/water solubility data, provide a good simulation of the system's vapor-liquid and solid-liquid equilibria. Urea growth and nucleation rate crystallization data obtained from the literature are provided for the crystallizer units.

Feature Highlights

PRO/II Case Book



Solids-Handling Application



User-supplied Solubility Data



Stoichiometric Reactor Units



Filtering Centrifuge Units



Solids Dryer and Freezer Units



Crystallizer Units with User-supplied Nucleation and Growth Rates

Urea Plant 5-1

Introduction What is Urea? Urea is a source of fixed nitrogen used primarily as a crop fertilizer and as a protein food supplement for livestock. Urea is particularly desirable for this use as it is readily soluble in water. A secondary use for urea is as a feedstock for the manufacture of adhesives, plastics and resins. Urea is manufactured by the high pressure reaction of ammonia and carbon dioxide to form ammonium carbamate, followed by the decomposition of the carbamate to yield urea and water. With recycle and a stoichiometric excess of feed components, about 99% of the CO2 and NH3 is converted to urea. The major contaminant is a dimer of urea called biuret (NH2CONHCONH2.H2O). The biuret concentration should not exceed 0.2-0.3% when the urea is to be used for feed supplements or as feedstock for plastics production. For fertilizer use, the biuret content may be up to 1%.

Relevance Urea has a maximum nitrogen content of 46% and, among major nitrogenous fertilizers, is second only to ammonia. It also has the highest nitrogen content of any solid fertilizer and can be easily manufactured as granules. Worldwide, in 2002 a total of about 108 million metric tons (108Mt) of urea were produced in more than 70 countries. This production delivered about 51.4Mt of contained nitrogen. China was the largest producer with about 28%, and all of asia accounted for about 46% of the total. The United States produced about 13%, or about 14Mt. Capacity in North America and Western Europe is expected to decline due to fluctuating natural gas prices. It is expected that production will continue to shift toward world regions that have abundant natural gas, lower-cost raw materials, and cheaper labor.

Routes to Urea The production of urea may be divided into two separate parts: Synthesis Finishing The synthesis loop produces a concentrated 70-80% urea solution. The finishing step produces either granular urea or crystalline urea. Spherical granules or flakes are formed by evaporation followed by 5-2 Urea Plant

March 5, 2014

passing the molten solid product countercurrent to a flow of hot air (known as prilling). Crystallization is used to produce virtually pure crystalline urea. The type of finishing process determines the final form of urea required (i.e., the biuret content, grain size, and moisture content). Once-through urea processes, now rare, were once common. In these plants, unconverted ammonia would be recovered and undergo downstream conversion to other ammonium compounds. Nowadays, partial and total recycle processes are used, with total recycle plants being more commonplace. Two types of urea manufacturing process obtained from the open literature are outlined below. Table 5-1: Types of Urea Manufacturing Processes Process

Description

Reference

Toyo Koatsu

Total recycle process using medium operating conditions (synthesis loop at 3500 psia, high pressure decomposer at 325 psia, low pressure decomposer at 25 psia). Produces prilled urea with 0.4 wt% biuret, and 0.3 wt% moisture.

Chao1 and Dente2

Snamprogetti

Total recycle process using mild operating conditions (synthesis loop at 2500 psia, high pressure decomposer at 260 psia, low pressure decomposer at 65 psia).

Hydrocarbon Processing6

In the United States, urea is produced mainly in the form of spherical prills or granules between 20 and 50 US. mesh in size, although the use of purer, crystalline urea is increasing rapidly.

Process Outline The urea process described in this case book produces a crystalline product, and is based on information obtained from Chao1 and Dente2. The urea process presented is intended as a generalized example of a urea flowsheet and does not represent any specific licensed technology. The urea flowsheet presented here is based on the plant described by Chao1 for the Toyo Koatsu process, which is a total NH3 recycle process. The urea synthesis plant modeled here is a partial NH3 recycle process. A schematic of the process is shown in Figure 5-1.

PRO/II Case Book

Urea Plant 5-3

Figure 5-1: Urea Plant Schematic

U r e a i s f o r med by reacting CO2 and NH3 at high temperature and high pressure to form ammonium carbamate urea, and water:

8NH 3 + 4CO 2 

3NH 2 COONH 4 + NH 2 COONH 4 +3H 2 O

(5-1)

This highly exothermic reaction goes almost to completion under reactor conditions of about 365 F and 3515 psia. The reactor product stream pressure is let down through a pressure control valve on the exit of the reactor. The reactor exit stream then enters the NH3 recovery column where recovered NH3 is recycled back to the reactor. The bottoms of the NH3 recovery column then enter the high pressure decomposer where a small fraction of the ammonium carbamate is decomposed and excess NH3 is removed as a vapor stream:

NH 2 COONH 4  NH 2 CONH 2 + H 2 O

(5-2)

This equilibrium endothermic decomposition reaction does not go to completion under normal reaction conditions of 302 F and 325 5-4 Urea Plant

March 5, 2014

psia. The exiting liquid then enters the low pressure decomposer where the majority of ammonium carbamate decomposes at 150 F and 25 psia, and a mixed NH3/H2O vapor is removed as a vapor stream. The liquid stream then enters a flash drum followed by an evaporator where additional NH3/H2O is removed as a vapor. The remaining liquid urea/H2O stream then enters the crystallization section. The crystallization scheme used involves the use of a vacuum, forced recirculation configuration. This concentrates the solution to supersaturation resulting in urea crystal formation. The first crystallizer operates at 130 F and 1.5 psia, while the second crystallizer operates at 130 F and 1.335 psia. Following each crystallization stage is a centrifuge which separates the crystal product from the mother liquor. The two stage crystallizer is then followed by a dryer to remove<%0> most of the <%-2>remaining water. This type of crystallization scheme requires significantly less energy compared to atmospheric configurations.

Process Simulation The complete input file for this simulation can be found in Appendix 5-B. Selected portions of the input file are shown here. For detailed explanations of the keywords used in the input file, please refer to the PRO/II Keyword Manual, available from Invensys.

KWM n appears beside some examples of keyword input. KWM indicates the PRO/II Key Word Manual, Thermo indicates the PRO/II Thermodynamic Data Input Manual, etc. “n” indicates the chapter that provides detailed explanation of the keyword entries.

PRO/II Case Book

Urea Plant 5-5

Simulation Model Figure 5-2 shows a block diagram of the simulation flowsheet. Figure 5-2: Urea Plant Simulation Flowsheet

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General Data English units of measure are used throughout the simulation for input and output report data. The density units are changed from the default API gravity units to DENSITY units (lb/ft3). The FLENGTH keyword is used to specify the fine length units of microns. The MBAL keyword specifies that an overall mass balance be reported in the final output.

KWM 5

DIMEN ENGLISH, XDEN=DENSITY, FLENGTH=MIC PRINT RATE=W, STREAM=COMPONENT, MBAL

Component Data All components except the intermediate, ammonium carbamate, are in the SimSci databank. Ammonium carbamate is specified to be a non-library component (using the NONLIB keyword). The particle size distribution intervals for urea are given using the ATTRIBUTE statement. The component urea is specified to exist in the vapor, liquid, and solid phases using the PHASE statement.

KWM 6

COMPONENT DATA LIBRARY 1, UREA / 2, WATER / 4, AMMONIA / 5, CO2 / & 6, N2 / 7, O2 / 8, H2, BANK=SIMSCI NONLIBRARY 3, AMCA PHASE VLS=1 ATTR COMP=1, PSD(MIC) 0, 20, 50, 100, 200, 500, 1000.

Literature data1,4 and the property estimation facilities of the Thermodynamics Data Manager (TDM program) are used to obtain physical property data for the intermediate compound ammonium carbamate. A portion of the physical property data input for this compound is shown below. $ $ $ $ $ $ $ $ $ $

PRO/II physical property insert for: Name: AMMONIUM CARBAMATE Formula: CH6N2O2 Created: 08/24/93 Source: User File: urea Thermo methods available for use: Library EOS Methods PHASE VLS = 3 MW 3, 0.7807092E+02 SPGR 3, 1.2 ACENTRIC 3, 0.5942138E+00 TC(K) 3, 0.6590952E+03 PC(PA) 3, 0.6740707E+07 FORMATION(S,J/KG,MOLE) 3, -.6450466E+09, -.4480641E+09

PRO/II Case Book

Urea Plant 5-7

NMP(K) 3, 0.4061500E+03 HFUS(J/KG,MOLE) 3, 0.6903593E+08 VP(L,PA,K) CORR=20, LN, DATA= 3, & 0.4261500E+03, 0.3031500E+03, -.2929800E+02, .3908196E+04, & 0.9295685E+01, -.1620786E-04, 0.2000000E+01, 0.1162653E07

Thermodynamic Data The NRTL liquid activity coefficient method is used to predict the vapor-liquid equilibria, while the Soave-Redlich-Kwong equation of state is used to calculate the liquid and vapor phase entropies. Transport properties are calculated using the LIBRARY method. User-supplied solubility data are used to predict solid-liquid solubilities.

KWM 8

THERMODYNAMIC DATA METHOD SYSTEM=NRTL, ENTROPY(V)=SRK, ENTROPY(L)=SRK, & KVALUE(SLE)=SOLDATA, TRANSPORT=LIBRARY

Solubility Data With many inorganic systems, ideal solubility does not adequately describe the solution behavior. For these cases solubility data can be fitted to the following equation:

ln  x i  = A + B ---- + C ln  T  T

(5-3)

The above equation provides a good fit to much of the solubility data reported in the literature. For systems containing more than one solvent, the solubility of the solute in the multi component solvent is calculated using the following relationship: N

x  i mix  =

 xj  xi·j 

ji

(5-4)

j=1

where:

xj x j = -------------------  N   x   j j = 1 

ji

(5-5)

The solubility expression and the mixing rule described in the above equations provide a great deal of flexibility in matching data 5-8 Urea Plant

March 5, 2014

reported in the literature and obtained in the plant. Solubility data for the urea/water solute/solvent pair are provided as shown below.

Thermo 7

KVALUE(SLE) SOLUTE 1 SOLDATA(K) 1,2, 0., -1310.37, 0.533619

Stream Data Feed Streams Data for the ammonia feed stream and the carbon dioxide feed stream are provided as shown below.

KWM 9.1

STREAM DATA PROP STRM=1, TEMP=-28, PRES=320, COMP(W)=4,105049 PROP STRM=2, TEMP=100, PRES=300, COMP(W)=5,93408

Recycle Streams The composition, temperature, and pressure of the recycle stream from the NH3 recovery column are estimated initially for the first run through the simulation. $ INITIAL GUESS FOR TEAR STREAMS

KWM 9.1

$ PROP STRM=7, TEMP=126, PRES=320, COMP(W)=2, 0.5 / 4, 58667.0

Reaction Data The stoichiometry of the two reactions—the primary urea reaction and the decomposition reaction<%-2>—is provided in the Reaction Data category of input.

KWM 10.8

PRO/II Case Book

RXDATA RXSET ID=RST1 REACTION ID=RXC1 STOICHIOMETRY 4,-8 / 5,-4 / 1,3 / 2,3 / 3,1 $ $ DECOMPOSITION REACTION $ RXSET ID=RST2 REACTION ID=RXC2 STOICHIOMETRY 3,-1 / 4,2 / 5,1

Urea Plant 5-9

Unit Operations Urea Synthesis As shown in Figure 5-2, fresh NH3 feed (stream 1) is mixed with recycle NH3 (stream 7) from the NH3 recovery column (COL1). The combined NH3 feed is raised to the operating pressure of reactor RX1 of 3515 psia in pump P1. Fresh CO2 feed (stream 2) is raised to the operating pressure of reactor RX1, 3516 psia, in compressor COM1. The primary urea reaction occurs in a high pressure, high temperature reactor. Reactor (RX1) is modeled as a conversion reactor unit, with 100% conversion. This reactor uses the reaction set RSTI previously defined in the Reaction Data category of input. Note that the heat of reaction may be optionally input for the urea reaction. However, PRO/II can calculate the heat of reaction from the heat of formation of the components if a value is not input.

KWM 14.2

CONREACTOR UID=RX1 FEED 3, 4 PRODUCT L=5 OPERATION ISOTHERMAL, PHASE=L, TEMP=365. RXCALC MODEL=STOIC RXSTOIC RXSET=RST1 REACTION RXC1 BASE COMPONENT=5 CONVERSION 1.0

High pressure reactor effluent is reduced in pressure to 320 psia through a valve (VL1) before entry into the NH3 recovery column (COL1). The column is simulated with the SHORTCUT column model. The column product specifications are 65% of the NH3 are recovered in the overhead product (stream 7), which is 99.995% ammonia. A bubble condenser is used for the overhead product.

KWM 12.8

SHORTCUT UID=COL1 FEED 6 PRODUCT STREAM=7, PRES=320, PERCENT(W)=23 PRODUCT STREAM=8, PRES=325 SPEC STREAM=7, COMP=4, FRACTION(W), VALUE=.99995 SPEC STREAM=7, COMP=4, RATE(W), RATIO, & STREAM=6, COMP=4, RATE(W), VALUE=0.65 CONDENSER TYPE=BUBBLE EVALUATE MODEL=CONVENTIONAL, KEYL=4, KEYH=2, RRMIN=2.5

The bottoms product from column COL1 (stream 8) is then sent to the high pressure and low pressure decomposers (RX2, RX3) modeled as conversion reactors. Both reactors use reaction set 5-10 Urea Plant

March 5, 2014

RST2 previously defined in the Reaction Data category of input. In the high pressure (325 psia) reactor, 88% of the carbamate is decomposed to urea under isothermal conditions at 302 F. An off gas of CO2 and NH3 is generated in streams 9 and 12. In the low pressure (25 psia) reactor, 99.95% of the remaining carbamate is converted to urea at 252 F.

KWM 14.2

KWM 11.1

KWM 14.2

CONREACTOR UID=RX2 FEED 8 PRODUCT V=9, L=10 OPERATION ISOTHERMAL, PHASE=L, TEMP=302. RXCALC MODEL=STOIC RXSTOIC RXSET=RST2 REACTION RXC2 BASE COMPONENT=3 CONVERSION 0.88 $ $ HIGH PRESSURE DECOMPOSER BOTTOMS COOLER $ FLASH UID=FL2 FEED 10 PRODUCT M=11 ISO TEMP=158, PRES=25 $ $ LOW PRESSURE DECOMPOSER $ CONREACTOR UID=RX3 FEED 11 PRODUCT V=12, L=13 OPERATION ISOTHERMAL, PHASE=L, TEMP=252. RXCALC MODEL=STOIC RXSTOIC RXSET=RST2 REACTION RXC2 BASE COMPONENT=3

The reaction product stream 13 is then sent into a flash drum (FL3) and evaporator (FL4), both modeled as flash units, where H2O and NH3 are taken off as a vapor in streams 14 and 16.

Finishing The bulk urea solution from the urea synthesis section is then sent into the first stage (CR1) of a two stage vacuum evaporative crystallization purification process. The crystallizer is operated at 130 F and 1.5 psia, and a design specification is made that 85% of the urea in the feed crystallizes. Growth and crystal nucleation rate data are provided using information obtained from the literature. See the Kinetic Data section later in this case book for more information on how these parameters were derived.

PRO/II Case Book

Urea Plant 5-11

Following the first crystallizer unit, the slurry is sent into a centrifuge (CEN1) to separate the crystal product from the mother liquor. The diameter of the centrifuge is specified to be 3 feet, and operates at a speed of 1000 RPM.

KWM 15.6

KWM 11.2

KWM 15.3

CRYSTALLIZER UID=CR1, NAME=CSTAGE1 FEED 18 PRODUCTS OVHD=19, BTMS=20 PRINT CSD OPERATION SOLUTE=1, SOLVENT=2, TEMP=130, PRES=1.5 DESIGN PFRAC=0.85 GROWTH KG=2.952E-8, GEXP=0. NUCLEATION KB=8.7417, BEXP=-3.87, 0., -1.75, 0. $ $ PUMP INTO FIRST CENTRIFUGE $ PUMP UID=P3, NAME=PUMP3 FEED 20 PRODUCT L=21 OPERATION PRES=20 $ $ FIRST STAGE CENTRIFUGE $ FCENTRIFUGE UID=CEN1, NAME=CENT1 FEED 21 PRODUCT FILTRATE=22, CAKE=23 RATING DIAMETER=3, RPM=1000

The mother liquor (stream 22) is then sent to the second stage crystallizer (CR2) and centrifuge (CEN2). The second crystallizer operates at the same temperature as the first, 130 F, but at a lower pressure, 1.335 psia.

KWM 15.6

KWM 11.2

KWM 15.3 5-12 Urea Plant

CRYSTALLIZER UID=CR2, NAME=CSTAGE2 FEED 22 PRODUCTS OVHD=24, BTMS=25 PRINT CSD OPERATION SOLUTE=1, SOLVENT=2, TEMP=130, PRES=1.335 DESIGN PFRAC=0.95 GROWTH KG=2.952E-8, GEXP=0. NUCLEATION KB=8.7417, BEXP=-3.87, 0., -1.75, 0. $ $ PUMP INTO SECOND CENTRIFUGE $ PUMP UID=P4, NAME=PUMP4 FEED 25 PRODUCT L=26 OPERATION PRES=20 $ $ SECOND STAGE CENTRIFUGE $ FCENTRIFUGE UID=CEN2, NAME=CENT2

March 5, 2014

FEED 26 PRODUCT FILTRATE=27, CAKE=28 RATING DIAMETER=3, RPM=1000

Both crystal product streams 23 and 28 are then sent to a dryer (DR1) where the final crystal product, containing 0.1% moisture by weight, is produced (stream 30).

KWM 15.1

$ $ FINAL DRYING OF SOLID PRODUCT $ DRYER UID=DR1, NAME=DRYER FEED 23, 28 PRODUCT OVHD=29, BTMS=30 OPERATION PRES=15 DESIGN BTMS, MOISTURE(W)=0.001

Finally, the solid urea crystals from the dryer are cooled to 200 F prior to prilling.

KWM 15.7

$MAKE SURE THAT ANY REMAINING UREA IS CONVERTED TO A SOLID $PRIOR TO CONVERSION TO A GRANULAR PRODUCT $ FREEZER UID=FRZ1, NAME=FREEZER FEED 30 PRODUCT M=31 OPERATION TEMP=200., DP=0.

The prilling section of the urea flowsheet, which converts the urea into a granular product, is not simulated in this case book.

Kinetic Data It is important to accurately determine growth and nucleation kinetic parameters. The article by Bennett3 is a good source of urea crystallization data. The articles by Bennett3 and Perry4 provide good discussions on calculation of crystallization kinetic parameters from crystal size distribution data. Crystal size distribution data obtained from the Bennett3 article for sample number 192 are used to demonstrate how to calculate both growth and nucleation rates. First, the crystal size distribution data in Tyler screen size are converted to average particle diameter. Table 5-2: Tyler Screen Sizes Screen Range

PRO/II Case Book

Length range (mm)

Average Diameter (mm)

14-20

1.168-0.833

1.000

20-28

0.833-0.589

0.711 Urea Plant 5-13

Table 5-2: Tyler Screen Sizes Screen Range

Length range (mm)

Average Diameter (mm)

28-35

0.589-0.417

0.503

35-48

0.417-0.295

0.356

48-65

0.295-0.208

0.251

65-100

0.208-0.147

0.178

Next the cumulative screen collection data must be converted into actual weight percent for each interval range. Table 5-3: Screen Collection Data Avg Diameter, Dav (mm)

Screen Accumulation

Weight Percent

1.000

4.4

4.4

0.711

18.8

14.4

0.503

43.0

24.2

0.356

74.6

31.6

0.251

90.1

15.5

0.178

97.5

7.4

-0.178

100.0

2.5

The number density (nL) as defined here is the number of crystals in a specified size range up to size L per liter of volume. The formal definition for n is: where:

nL =

N lim  --------  l  0 L

(5-6)

N = number of crystals retained on the screen in the specified size range

L = difference between the screen size of the retaining sieve and its immediate predecessor. As an example, the number density for screen size 14-20 (n20) is calculated directly using the following slurry properties and the above screen data. Slurry density, MT = 450. g/L 5-14 Urea Plant

March 5, 2014

Crystal density, rc = 1.335 g/cm3 = 1.335x10-3 g/mm3 Retention time, t = 3.38 h

L = 1.168-0.833 = 0.335 mm Crystal volume, Vc = Dav3

Now, nL is given by: where:

M T x wt n L = ------------------ c V c L

(5-7)

xwt = weight fraction retained on screen So for example, the number of crystals / mm L

450  0.044  n 20 = ----------------------------------------------------------------------------------- = 44273 –3  1.335 10   1.168 – 0.833   1.0 

(5-8)

ln(n20) = 10.698 Similar calculations for the other screen sizes yield the following table. Table 5-4: Crystal Number Density Avg Diameter, Dav (mm)

Number Density (n)

ln(n)

0.178 0.251 0.356 0.503 0.711 1.000

72492960 37958350 19346070 3726570 553490 44773

18.099 17.452 16.778 15.131 13.224 10.698

A plot of the natural log of number density versus the average particle diameter is known as a Population Density Plot. An example is shown in) as shown in Figure 3. The intercept of this plot, n0, is known as the nuclei population density. When using the following relationships, both the nucleation and growth rates are calculated.

– D av 0 ln  n  = ----------- + ln  n  Gt B = Gn PRO/II Case Book

0

(5-9)

Urea Plant 5-15

where: Dav= average crystal diameter G= growth rate over the time interval t t= crystallizer time interval n0= number density of crystal nuclei B = nucleation rate

Figure 5-3: Population Density Plot

From Figure 5-3, the intercept is 19.78 and the slope is -9.13. The following calculations then are performed. Since Dav= 1 mm and slope = -Dav/Gt It follows that:

5-16 Urea Plant

Slope = -1/Gt = -9.13

March 5, 2014

Therefore: G = 1/(-9.13)(3.38) = 0.0324 mm/h The growth rate calculated using equation Equation 5-9 is: B = (0.0324) * exp(19.78) = 12.65x106 crystals / L-h The nuclei number density is also given by:

n where:

0

k i–1 = Kb MT G

(5-10)

Kb = a constant i, k = exponents (constants) Table 5-5 lists a group of samples reported by Bennettt3 that characterizes observed growth and nucleation rates. Table 5-5: Growth Versus Nucleation Rate Sample No.

ln(n0)

G

ln G

191 192 193 194

18.18 19.71 18.70 20.51

0.0330 0.0338 0.0317 0.0200

-3.41 -3-39 -3.45 -3.91

Using the natural logarithms of growth vs. nuclei number, densities are plotted as shown in Figure 5-4. Using the following expression and the resulting slope of the plot, the exponent for the power law nucleation rate equation is determined. Calculation of the i exponent assumes the slurry density (MT) is constant.

PRO/II Case Book

Urea Plant 5-17

Figure 5-4: Growth vs. Nucleation Rate

The slope (-2.75) of the plot shown in Figure 5-4 yields a value of -1.75 for the exponent i. The nucleation rate, B, then is obtained from Equation 5-11 as: k

B = Kb MT G

– 1.75

(5-11)

Similar data at constant growth rate is required to calculate the k exponent in the final form of the nucleation equation. For urea crystallization, a value of -3.87 is recommended for the k exponent by Bennett3. In addition, a value of -1.66 is recommended for the i exponent, compared to -1.75 calculated here. The paper by Garside and Shaw5 is a recommended source of nucleation and growth kinetic data. The following is the final recommended form of the nucleation equation as reported by Garside and Shaw5. – 3.87

B = 0.548M T

G

– 1.66

(5-12)

The units of the nucleation rate, B, are Number of crystals/L-s. The constants of this equation must be converted to be consistent with input units (refer to Table 4.1 of the PRO/II Keyword Input Manual for default dimensional units). The following summarizes the

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default dimensional units used in the growth and nucleation expressions. PRO/II Growth Rate Expression:

G = K a SSRATIO

G exp onent

(5-13)

Term

Units

G

velocity

Kg, constant

velocity

SSRATIO, supersaturation

dimensionless

PRO/II Nucleation Rate Expression j

i

K

B = K b M T SSRATIO G RPM

1

(5-14)

Term

Units

B

No. / [(time) (liquid volume)]

Kb, constant

No. / [(time) (liquid volume)]

MT

liquid density

RPM

revolutions per minute

The GEXPONENT term in Equation 5-13 is set to zero. The following are converted growth and nucleation rates.

0.0324mm m ft h G = K a = --------------------------  ----------------------  3.28 ----  -------------h 1000mm m 3600s – 8 ft = 2.952 10 ---s L 6 number of crystals B = 12.65 10 -----------------------------------------------  28.32 -----3L-h ft number of crystals= 3.582 10 ---------------------------------------------3 ft h 8

(5-15)

(5-16)

Next, the Kb constant in the nucleation expression, Equation 5-14, must be converted to be consistent with input units in the following manner. 3 i

0.0624262lb  ft i g i i g M T  --- = M T ---  ---------------------------------------- L L gL = 0.0624262 PRO/II Case Book

i

lb i i  M T   -----3-  

(5-17)

ft

Urea Plant 5-19

i m k k m 3.28ft G  ---- = G ----  --------------  s s m 

k

k k ft k =  3.28 G  ----  s

No No L s K b  ------------ = K b  ------------ 28.32 -----3- 3600  ---  L – s  L – s  h ft

(5-18)

(5-19)

3

= 101952K b  Number of crystals/ft h  Now, using equation (13):

B =   0.548 101952 0.0624262

3.87

– 3.87

= 8.7417  M T

 3.28 

G

1.66

3.87

 M T G

– 1.66

– 1.66 (5-20)

where units of measure are: B (Number of crystals/ft3-h) G (ft/s)Ncx = abbreviation for number of crystals MT (lb/ft3)

This newly formulated equation can now be tested to check that it fits the published nucleation rate data using the reported slurry density of 450 g/L and calculated growth rate of 2.952x10-8 ft/s. 3

 N cx  ft  g B = 8.74172  450 --- 0.0624262  -------------------  L  g  L 

– 3.87 – 8 – 1.66

 2.952 10 

(5-21)

7  Number

of crystals = 6.842289 10 --------------------------------------------3   ft h There is a large deviation in nucleation rate compared to the value of 3.582x108 number of crystals/ft3-h calculated from the published data. However, if the calculated growth rate exponent of -1.75 is used in place of the suggested value of -1.66, the nucleation rate is calculated to be 3.258x108 number of crystals/ft3-h. This value compares closely with the value calculated from the data. The final form of growth and nucleation rate equations used in this simulation then are: –8

G = 2.952 10

B =

5-20 Urea Plant

– 3.87 – 1.75 8.741M T G

(5-22)

March 5, 2014

Technical Results The overall mass balance for the partial NH3 recycle urea plant is summarized in the output report of the simulation: OVERALL PLANT MASS BALANCE ------------------ LB/HR ------------------ PERCENT COMPONENT FEED +REACTION -PRODUCT =DEVIATION DEV --------------------- ---------- ---------- ---------- ---------- ------1 UREA 0.00 95598.21 95598.21 0.00 0.00 2 WATER 0.00 28677.21 28677.21 0.00 0.00 3 AMCA 0.00 3542.12 3542.55 -0.43 -0.01 4 AMMONIA 105049.00 -55764.79 49269.20 15.01 0.03 5 CO2 93408.00 -72052.75 21355.25 0.00 0.00 6 N2 0.00 0.00 0.00 0.00 0.00 7 O2 0.00 0.00 0.00 0.00 0.00 8 H2 0.00 0.00 0.00 0.00 0.00 TOTAL

198457.00

0.00 198442.42

14.58

0.01

Conclusion The 1000 tons/day urea process discussed in this case book demonstrates the use of many chemicals and solids capabilities in PRO/II. This example also highlights those features of PRO/II that make it easy to incorporate available literature data.

Output Results The keyword input file appears in Appendix 5-A. Appendix 5-B is a listing of selected results. These include the urea reactor RX1 and the decomposers RX2 and RX3, the filtering centrifuge units CEN1 and CEN2, the dryer DR1, the crystallizers CR1 and CR2, the solids freezer FRZ1, and stream weight component rates for selected streams.

PRO/II Case Book

Urea Plant 5-21

References 1. 2.

Chao, George Tsei-Yu, “Urea: Its Properties and Manufacture”, Chao's Institute, 1967. Dente, M., S. Pierucci, A. Sogaro, G. Carloni, E. Rigolli, “Simulation Program For Urea Plants”, Comput. Chem. Eng. Vol 12, No. 5, pp. 389-400, 1988.

3.

Bennett, R.C., M. VanBuren, “Commercial Urea Crystallization”, Crystallization From Solutions and Melts, Chem. Eng. Prog. Symp. Ser., No. 95(7), Vol. 65, 1969.

4.

Perry, R.H., D. Green, “Perry's Chemical Engineers' Handbook”, Sixth Edition, pp. 19-32 - 19-33, McGraw Hill, 1984.

5.

Garside, J., M.B. Shah, “Crystallization Kinetics From MSMPR Crystallizers”, Ind. Eng. Chem. Process Des. Dev., Vol 19, No 4, pp. 509-514, 1980.

6.

Hydrocarbon Processing, Nov. 1985, pp. 172.

7.

Austin, G.T., “Shreve's Chemical Process Industries,” Fifth Edition, pp.311-13, McGraw-Hill, 1984.

The following are additional sources of information related to using PRO/II with solids and electrolytes: 8.

Goldfarb, S., J. Coon, J. Tanger, K.M. Ng, C.F. Chu, “Crystallization Process Optimization Using PRO/II”, Presented at: November 1990 AIChE Meeting.

9.

Goldfarb, S., J. Coon, J. Tanger, A. Harvey, “Rigorous Simulation of Aqueous Electrolyte Flowsheets With Special Emphasis on Solids Processing Capabilities”, Presented at: Fourth International Symposium on Process Systems Engineering (PSE 91).

10. Goldfarb, S., “Continuous Sugar Crystallization Process With Applications in the Agri-Chemical Industry,” Presented at: August 1993 AIChE Meeting.

5-22 Urea Plant

March 5, 2014

Appendix 5-A: Input Data File The keyword input file for this example is UreaPlnt.inp. It normally is installed with the PRO/II Casebook manual in the folder: %ProIIInstall%\Manual\Casebook\Inputs\

where %ProIIInstall% represents the root directory where PRO/II is installed. The following is a listing of that keyword input file. $ UREA PLANT FLOWSHEET $ TITLE PROJ=CaseBook, PROBLEM=UreaPlant, USER=SimSci, DATE=Apr_2010 DIMEN ENGLISH, XDEN=DENSITY, FLENGTH=MIC PRINT RATE=W, STREAM=COMPONENT, MBAL CALCULATION TRIALS=50 TOLERANCE STREAM=0.001 $ COMPONENT DATA LIBRARY 1, UREA / 2, WATER / 4, AMMONIA / 5, CO2 / 6, N2 / & 7, O2 / 8, H2, BANK=SIMSCI NONLIBRARY 3, AMCA PHASE VLS=1 ATTR COMP=1, PSD(MIC) 0, 20, 50, 100, 200, 500, 1000. $ $ Fill in missing data for UREA and AMMONIUM CARBAMATE from the Thermodynamic Data Manager. $ $ PRO/II physical property insert for: $ Name: UREA $ Formula: CH4N2O $ Created: 05/10/95 $ Source: User File: urea $ ACENTRIC 1, 0.5973908E+00 SURFACE(L,N/M,K) CORR= 1, DATA= 1, 0.5000000E+03, & 0.2000000E+03, 0.1565836E+00, -.2684714E-03, & 0.1951699E-07, 0.9796545E-10, -.1376130E-12, & 0.1206885E-15 VISC(V,PAS,K) CORR= 1, DATA= 1, 0.5000000E+03, & 0.2000000E+03, -.1111774E-05, 0.2164776E-07, & 0.2485747E-14, -.8143611E-17, 0.1319303E-19, & -.8382776E-23 VISC(L,PAS,K) CORR=20, DATA= 1, 0.5000000E+03, & 0.2000000E+03, -.1761028E+03, 0.1244212E+05, & 0.2315481E+02, 0.0000000E+00, 0.0000000E+00, & 0.0000000E+00 COND(V,W/MK,K) CORR= 1, DATA= 1, 0.5000000E+03, & 0.2500000E+03, -.1894533E-01, 0.7768554E-04, & PRO/II Case Book

Urea Plant 5-23

-.8991741E-11, 0.2449163E-13, -.3284755E-16, & 0.1733994E-19 COND(L,W/MK,K) CORR= 1, DATA= 1, 0.5000000E+03, & 0.2000000E+03, 0.2532868E+00, -.1769604E-03, & -.1309749E-06, 0.0000000E+00, 0.0000000E+00, & 0.0000000E+00

$ $ PRO/II physical property insert for: $ Name: AMMONIUM CARBAMATE $ Formula: CH6N2O2 $ Created: 05/10/95 $ Source: User File: urea $ $ Thermo methods available for use: $ Library $ EOS Methods $ PHASE VLS = 3 MW 3, 0.7807092E+02 SPGR 3, 1.2 ACENTRIC 3, 0.5942138E+00 TC(K) 3, 0.6590952E+03 PC(PA) 3, 0.6740707E+07 FORMATION(S,J/KG,MOLE) 3, -.6450466E+09, -.4480641E+09 NMP(K) 3, 0.4061500E+03 HFUS(J/KG,MOLE) 3, 0.6903593E+08 VP(L,PA,K) CORR=20, LN, DATA= 3, 0.4261500E+03, & 0.3031500E+03, -.2929800E+02, -.3908196E+04, & 0.9295685E+01, -.1620786E-04, 0.2000000E+01, & 0.1162653E-07 LATENT(J/KG,K,MOLE) CORR= 1, DATA= 3, 0.6000000E+03, & 0.4000000E+03, 0.5178937E+09, -.4814254E+07, & 0.2047703E+05, -.4408357E+02, 0.4744715E-01, & -.2057343E-04 VISC(L,PAS,K) CORR=20, DATA= 3, 0.5000000E+03, & 0.2500000E+03, -.4705848E+02, 0.4595930E+04, & 0.4787454E+01, 0.0000000E+00, 0.0000000E+00, & 0.0000000E+00 SURFACE(L,N/M,K) CORR= 1, DATA= 3, 0.5000000E+03, & 0.2000000E+03, 0.8006542E-02, -.1452831E-04, & 0.2243716E-10, 0.9652577E-11, -.1462233E-13, & 0.1190758E-16 ENTH(L,J/KG,K,MOLE) CORR=1, DATA= 3, 0.2955000E+03, & 0.1255000E+02, -.1765825E+08, -.6685015E+04, & 0.3085568E+03, -.1735744E+00, -.1174778E-08, & 0.1799982E-11 ENTH(V,J/KG,K,MOLE) CORR=1, DATA= 3, 0.1500000E+04, & 0.1500000E+03, 0.9131459E+08, 0.2351811E+05, & 0.7600609E+02, 0.7937258E-02, -.2484022E-04, & 0.7275022E-08 DENS(L,KG/M3,K,MOLE) CORR=1, DATA=3, 0.4775945E+03, & 0.3664834E+03, 0.2375940E+02, -.4553412E-01, & 0.1678109E-03, -.4529840E-06, 0.6004568E-09, & 5-24 Urea Plant

March 5, 2014

-.3358131E-12 VISC(V,PAS,K) CORR= 1, DATA= 3, 0.5000000E+03, & 0.2000000E+03, -.1917443E+00, 0.3993549E-02, & 0.3461876E-09, -.1233446E-11, 0.2128086E-14, & -.1416680E-17 COND(V,W/MK,K) CORR= 1, DATA= 3, 0.5000000E+03, & 0.2500000E+03, -.1232028E+00, 0.1417707E-02, & -.6673806E-05, 0.1653591E-07, -.2039134E-10, & 0.1002095E-13 COND(L,W/MK,K) CORR= 1, DATA= 3, 0.5000000E+03, & 0.2000000E+03, 0.2532868E+00, -.1769604E-03, & -.1309749E-06, 0.0000000E+00, 0.0000000E+00, & 0.0000000E+00 CP(S,J/KG,K,MOLE) CORR=1, DATA= 3, 0.4731500E+03, & 0.2931500E+03, 0.9867493E+06, -.1073353E+05, & 0.4725547E+02, -.8751843E-01, 0.5856834E-04, & 0.0000000E+00 DENS(S,KG/M3,K,MOLE) CORR=1, DATA=3, 0.2931500E+03,& 0.2931500E+03, 0.2222994E+02, 0.0000000E+00, & 0.0000000E+00, 0.0000000E+00, 0.0000000E+00, & 0.0000000E+00 SVTB 3, -.1348239E+02 SLTB 3, 0.9952457E+02 SLTM 3, 0.1659695E+02 HVTB 3, -.1246233E+02 HLTB 3, 0.4591732E+05 HLTM 3, 0.8994148E+04

$ THERMODYNAMIC DATA METHOD SYSTEM=NRTL, ENTROPY(V)=SRK, ENTROPY(L)=SRK, & KVALUE(SLE)=SOLDATA, TRANSPORT=LIBRARY KVALUE(SLE) SOLUTE 1 SOLDATA(K) 1,2, 0., -1310.37, 0.533619 $ STREAM DATA PROP STRM=1, TEMP=-28, PRES=320, COMP(W)=4,105049 PROP STRM=2, TEMP=100, PRES=300, COMP(W)=5,93408 $ $ INITIAL GUESS FOR TEAR STREAMS $ PROP STRM=7, TEMP=126, PRES=320, COMP(W)=2,0.5 / 4,58667. NAME 1, NH3FD / 2, CO2FD / 9, DECGS1 / 12, DECGS2 / & 14, FLGS1 /16, FLGS2 /19, CRYGS1 / 24, CRYGS2 / & 29, DRYGS /31, UREAPROD $ $ REACTION DATA $ RXDATA $ $ MAIN UREA REACTION $ RXSET ID=RST1 PRO/II Case Book

Urea Plant 5-25

REACTION ID=RXC1 STOICHIOMETRY 4,-8 / 5,-4 / 1,3 / 2,3 / 3,1

$ $ DECOMPOSITION REACTION $ RXSET ID=RST2 REACTION ID=RXC2 STOICHIOMETRY 3,-1 / 4,2 / 5,1 $ UNIT OPERATIONS $ $ CO2 COMPRESSOR $ COMPRESSOR UID=COM1 FEED 2 PRODUCT V=4 OPERATION PRES=3516, EFF=75 COOLER ACDP=1, ACTOUT=100 $ $ NH3 RECYCLE & FEED PUMP $ PUMP UID=P1 FEED 1, 7 PRODUCT L=3 OPERATION PRES=3515 $ $ HIGH PRESSURE REACTOR $ CONREACTOR UID=RX1 FEED 3, 4 PRODUCT L=5 OPERATION ISOTHERMAL, PHASE=L, TEMP=365. RXCALC MODEL=STOIC RXSTOIC RXSET=RST1 REACTION RXC1 BASE COMPONENT=5 CONVERSION 1.0 $ $ PRESSURE REDUCTION VALVE $ VALVE UID=VL1 FEED 5 PRODUCT M=6 OPER PRES=320 $ $ AMMONIA SEPARATOR $ SHORTCUT UID=COL1 FEED 6 PRODUCT STREAM=7, PRES=320, PERCENT(W)=23 PRODUCT STREAM=8, PRES=325 SPEC STREAM=7, COMP=4 , FRACTION(W), VALUE=.99995 SPEC STREAM=7, COMP=4 , RATE(W), RATIO, & 5-26 Urea Plant

March 5, 2014

STREAM=6, COMP=4, RATE(W), VALUE=0.65 CONDENSER TYPE=BUBBLE EVALUATE MODEL=CONVENTIONAL, KEYL=4, KEYH=2, RRMIN=2.5

$ $ HIGH PRESSURE DECOMPOSER $ CONREACTOR UID=RX2 FEED 8 PRODUCT V=9, L=10 OPERATION ISOTHERMAL, PHASE=L, TEMP=302. RXCALC MODEL=STOIC RXSTOIC RXSET=RST2 REACTION RXC2 BASE COMPONENT=3 CONVERSION 0.88 $ $ HIGH PRESSURE DECOMPOSER BOTTOMS COOLER $ FLASH UID=FL2 FEED 10 PRODUCT M=11 ISO TEMP=158, PRES=25 $ $ LOW PRESSURE DECOMPOSER $ CONREACTOR UID=RX3 FEED 11 PRODUCT V=12, L=13 OPERATION ISOTHERMAL, PHASE=L, TEMP=252. RXCALC MODEL=STOIC RXSTOIC RXSET=RST2 REACTION RXC2 BASE COMPONENT=3 CONVERSION 0.9995 $ $ FLASH DRUM $ FLASH UID=FL3 FEED 13 PRODUCT V=14, L=15 ISO TEMP=250, PRES=15 $ $ EVAPORATOR $ FLASH UID=FL4 FEED 15 PRODUCT V=16, L=17 TPSPEC TEMP=230 SPEC STREAM=17, FRAC(W), COMP=4, VALUE=0.001

PRO/II Case Book

Urea Plant 5-27

$ $ PUMP INTO FIRST CRYSTALLIZER $ PUMP UID=P2, NAME=PUMP2 FEED 17 PRODUCT L=18 OPERATION PRES=20 $ $ FIRST STAGE CRYSTALLIZER $ CRYSTALLIZER UID=CR1, NAME=CSTAGE1 FEED 18 PRODUCTS OVHD=19, BTMS=20 PRINT CSD OPERATION SOLUTE=1, SOLVENT=2, TEMP=130, PRES=1.5 DESIGN PFRAC=0.85 GROWTH KG=2.952E-8, GEXP=0. NUCLEATION KB=8.7417, BEXP=-3.87, 0., -1.75, 0. $ $ PUMP INTO FIRST CENTRIFUGE $ PUMP UID=P3, NAME=PUMP3 FEED 20 PRODUCT L=21 OPERATION PRES=20 $ $ FIRST STAGE CENTRIFUGE $ FCENTRIFUGE UID=CEN1, NAME=CENT1 FEED 21 PRODUCT FILTRATE=22, CAKE=23 RATING DIAMETER=3, RPM=1000 $ $ SECOND STAGE CRYSTALLIZER $ CRYSTALLIZER UID=CR2, NAME=CSTAGE2 FEED 22 PRODUCTS OVHD=24, BTMS=25 PRINT CSD OPERATION SOLUTE=1, SOLVENT=2, TEMP=130, PRES=1.335 DESIGN PFRAC=0.95 GROWTH KG=2.952E-8, GEXP=0. NUCLEATION KB=8.7417, BEXP=-3.87, 0., -1.75, 0. $ $ PUMP INTO SECOND CENTRIFUGE $ PUMP UID=P4, NAME=PUMP4 FEED 25 PRODUCT L=26 OPERATION PRES=20

5-28 Urea Plant

March 5, 2014

$ $ SECOND STAGE CENTRIFUGE $ FCENTRIFUGE UID=CEN2, NAME=CENT2 FEED 26 PRODUCT FILTRATE=27, CAKE=28 RATING DIAMETER=3, RPM=1000 $ $ FINAL DRYING OF SOLID PRODUCT $ DRYER UID=DR1, NAME=DRYER FEED 23, 28 PRODUCT OVHD=29, BTMS=30 OPERATION PRES=15 DESIGN BTMS, MOISTURE(W)=0.001 $ $ ENSURE ANY REMAINING UREA IS CONVERTED TO A SOLID $ FREEZER UID=FRZ1, NAME=FREEZER FEED 30 PRODUCT M=31 OPERATION TEMP=200., DP=0. $ END

PRO/II Case Book

Urea Plant 5-29

Appendix 5-B: Output Report File Selected PRO/II output is shown below. The output selected highlights solids capabilities. SIMULATION SCIENCES INC. PROJECT CaseBook PROBLEM UreaPlant

R PAGE P-4 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci PLANT MATERIAL BALANCE Apr_2010 ============================================================================== FEED STREAMS: 1 2 PRODUCT STREAMS: 9 12 14 16 19 24 29 31 27 OVERALL PLANT MOLAR BALANCE ---------------- LB-MOL/HR ---------------- PERCENT COMPONENT FEED +REACTION -PRODUCT =DEVIATION DEV --------------------- ---------- ---------- ---------- ---------- ------1 UREA 0.000 1591.827 1591.827 0.000 0.00 2 WATER 0.000 1591.827 1591.827 0.000 0.00 3 AMCA 0.000 45.371 45.376 -0.006 -0.01 4 AMMONIA 6168.265 -3274.396 2892.988 0.881 0.03 5 CO2 2122.436 -1637.198 485.239 0.000 0.00 6 N2 0.000 0.000 0.000 0.000 0.00 7 O2 0.000 0.000 0.000 0.000 0.00 8 H2 0.000 0.000 0.000 0.000 0.00 TOTAL

8290.701 -1682.568

6607.257

0.876

0.01

OVERALL PLANT MASS BALANCE ------------------ LB/HR ------------------ PERCENT COMPONENT FEED +REACTION -PRODUCT =DEVIATION DEV --------------------- ---------- ---------- ---------- ---------- ------1 UREA 0.00 95598.21 95598.21 0.00 0.00 2 WATER 0.00 28677.21 28677.21 0.00 0.00 3 AMCA 0.00 3542.12 3542.55 -0.43 -0.01 4 AMMONIA 105049.00 -55764.79 49269.20 15.01 0.03 5 CO2 93408.00 -72052.75 21355.25 0.00 0.00 6 N2 0.00 0.00 0.00 0.00 0.00 7 O2 0.00 0.00 0.00 0.00 0.00 8 H2 0.00 0.00 0.00 0.00 0.00 TOTAL

5-30 Urea Plant

198457.00

0.00 198442.42

14.58

0.01

March 5, 2014

SIMULATION SCIENCES INC. PROJECT CaseBook PROBLEM UreaPlant

R PAGE P-13 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci FILTERING CENTRIFUGE SUMMARY Apr_2010 ============================================================================== UNIT 14, 'CEN1', 'CENT1' Feeds

21

Products Liquid Mixed

22 23

Type of Operation

Rating

Operating Conditions Temperature, F Pressure, PSIA Average Particle Diameter, MIC Average Solid Density, LB/FT3 Total Solid Feed Mass Flow Rate, LB/HR Surface tension, DYNE/CM Volume Flow Rate of Filtrate, FT3/HR Particle Sphericity

130.0609 20.0000 648.4185 83.3434 6.429E+04 69.3608 589.9697 0.7500

Physical Configuration Bowl Diameter, FT Radius of Liquid Surface / Radius of Bowl Radius of Cake / Radius of Bowl Height of Bowl / Radius of Bowl RPM Basket Height, FT Selected Bowl Radius, FT Centrifuge Type

3.0000 0.7380 0.7900 0.9545 1000.0000 1.4317 1.5000 Not Specified

Cake Properties Mass Fraction of Solid in Cake Cake Thickness, MIC Cake Resistance, FT/LB Filter Medium Resistance, 1/FT Porosity if Cake

PRO/II Case Book

0.9523 9.601E+04 2.976E+06 6.096E+05 0.4500

Urea Plant 5-31


R PAGE P-14 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci FILTERING CENTRIFUGE SUMMARY Apr_2010 ============================================================================== UNIT 17, 'CEN2', 'CENT2' Feeds

26

Products Liquid Mixed

27 28

Type of Operation

Rating

Operating Conditions Temperature, F Pressure, PSIA Average Particle Diameter, MIC Average Solid Density, LB/FT3 Total Solid Feed Mass Flow Rate, LB/HR Surface tension, DYNE/CM Volume Flow Rate of Filtrate, FT3/HR Particle Sphericity

130.0768 20.0000 567.6160 83.3434 1.576E+04 69.4362 257.6413 0.7500

Physical Configuration Bowl Diameter, FT Radius of Liquid Surface / Radius of Bowl Radius of Cake / Radius of Bowl Height of Bowl / Radius of Bowl RPM Basket Height, FT Selected Bowl Radius, FT Centrifuge Type

3.0000 0.7380 0.7900 0.9545 1000.0000 1.4317 1.5000 Not Specified

Cake Properties Mass Fraction of Solid in Cake Cake Thickness, MIC Cake Resistance, FT/LB Filter Medium Resistance, 1/FT Porosity if Cake

5-32 Urea Plant

0.9482 9.601E+04 2.976E+06 6.096E+05 0.4500

March 5, 2014


R PAGE P-15 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci DRYER SUMMARY Apr_2010 ============================================================================== UNIT 18, 'DR1', 'DRYER' Feeds Products Vapor Mixed TEMPERATURE, DEG F PRESSURE, PSIA PRESSURE DROP, PSI MOLE FRAC VAPOR MOLE FRAC TOTAL LIQUID MOLE FRAC H/C LIQUID MOLE FRAC FREE WATER MOLE FRAC MW SOLID MOISTURE CONTENT DUTY, MM BTU/HR DRYER OPERATION

PRO/II Case Book

23

28

29 30 369.532 15.000 5.000 0.04528 0.03534 0.03534 0.00000 0.91937 9.99999E-04 10.55778 MOISTURE-P

Urea Plant 5-33


R PAGE P-16 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci CRYSTALLIZER SUMMARY Apr_2010 ============================================================================== UNIT 12, 'CR1', 'CSTAGE1' Feeds 18 Products Vapor 19 Mixed 20 OPERATING CONDITIONS TEMPERATURE, F 130.00 PRESSURE, PSIA 1.50 HEAT EXCHANGER DUTY, MM BTU/HR -11.9173 VOLUME, FT3 10745.9867 RESIDENCE TIME, HR 7.6394 CRYSTAL PRODUCTION RATE, LB/HR 64294.794 TEMPERATURE CHANGE IN HEAT EXCHANGER, F N/A SLURRY RECIRCULATION RATE, FT3/HR N/A AGITATOR RPM 100.000 CRYSTALLIZER DATA CRYSTAL COMPONENT SUPERSATURATION CRYSTAL SHAPE FACTOR

1

SLURRY PROPERTIES FEED SLURRY LIQUID VOLUME FRACTION FEED SLURRY VOLUMETRIC RATE, FT3/HR PRODUCT SLURRY LIQUID VOLUME FRACTION PRODUCT SLURRY VOLUMETRIC RATE, FT3/HR PRODUCT SLURRY MAGMA DENSITY, LB/FT3 KINETICS DATA GROWTH RATE, FT/SEC NUCLEATION RATE, NUMBER/HR/FT3

UREA 5.9605E-10 1.000 1.000 1494.103 0.452 1406.645 45.708 2.9520E-08 4.9515E+07

PARTICLE SIZE DISTRIBUTION ------- DIAMETER, MIC -------RANGE AVERAGE ------------------ ---------0.000 - 20.00 10.00 20.00 - 50.00 35.00 50.00 - 100.0 75.00 100.0 - 200.0 150.0 200.0 - 500.0 350.0 0.500 - 1.000 E+03 0.750 E+03

5-34 Urea Plant

--- WT FRAC ---FEED PRODUCT ------- ------0.0000 0.0000 0.0000 0.0001 0.0000 0.0012 0.0000 0.0136 0.0000 0.2314 0.0000 0.7537

---- NUMBER DENSITY ---/MIC/FT3 FEED PRODUCT ----------- ----------0.0000E+00 6.6295E+05 0.0000E+00 5.9924E+05 0.0000E+00 5.0980E+05 0.0000E+00 3.7651E+05 0.0000E+00 1.6779E+05 0.0000E+00 3.3323E+04

March 5, 2014


R PAGE P-18 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci CRYSTALLIZER SUMMARY Apr_2010 ============================================================================== UNIT 15, 'CR2', 'CSTAGE2' Feeds

22

Products Vapor Mixed

24 25

OPERATING CONDITIONS TEMPERATURE, F PRESSURE, PSIA HEAT EXCHANGER DUTY, MM BTU/HR VOLUME, FT3 RESIDENCE TIME, HR CRYSTAL PRODUCTION RATE, LB/HR TEMPERATURE CHANGE IN HEAT EXCHANGER, F SLURRY RECIRCULATION RATE, FT3/HR AGITATOR RPM

130.00 1.34 5.5558 2318.0340 5.0517 15763.480 N/A N/A 100.000

CRYSTALLIZER DATA CRYSTAL COMPONENT SUPERSATURATION CRYSTAL SHAPE FACTOR

1

UREA 1.7764E-17 1.000

SLURRY PROPERTIES FEED SLURRY LIQUID VOLUME FRACTION FEED SLURRY VOLUMETRIC RATE, FT3/HR PRODUCT SLURRY LIQUID VOLUME FRACTION PRODUCT SLURRY VOLUMETRIC RATE, FT3/HR PRODUCT SLURRY MAGMA DENSITY, LB/FT3

1.000 589.970 0.588 458.865 34.353

KINETICS DATA GROWTH RATE, FT/SEC NUCLEATION RATE, NUMBER/HR/FT3

PRO/II Case Book

2.9520E-08 1.4952E+08

Urea Plant 5-35


R PAGE P-19 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci CRYSTALLIZER SUMMARY Apr_2010 ============================================================================== UNIT 15, 'CR2', 'CSTAGE2' (Cont) PARTICLE SIZE DISTRIBUTION ------- DIAMETER, MIC -------RANGE AVERAGE ------------------ ---------0.000 - 20.00 10.00 20.00 - 50.00 35.00 50.00 - 100.0 75.00 100.0 - 200.0 150.0 200.0 - 500.0 350.0 0.500 - 1.000 E+03 0.750 E+03

--- WT FRAC ---FEED PRODUCT ------- ------0.0000 0.0000 0.0000 0.0003 0.0000 0.0035 0.0000 0.0353 0.0000 0.3966 0.0000 0.5643

---- NUMBER DENSITY ---/MIC/FT3 FEED PRODUCT ----------- ----------0.0000E+00 2.5525E+06 0.0000E+00 2.1909E+06 0.0000E+00 1.7158E+06 0.0000E+00 1.0849E+06 0.0000E+00 3.1958E+05 0.0000E+00 2.7730E+04


R PAGE P-20 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci MELTER/FREEZER SUMMARY Apr_2010 ============================================================================== UNIT 19, 'FRZ1', 'FREEZER' Feeds 30 Products Mixed

31

OPERATING CONDITIONS TEMPERATURE, F PRESSURE, PSIA PRESSURE DROP, PSI DUTY, MM BTU/HR MOLE FRAC VAPOR MOLE FRAC TOTAL LIQUID MOLE FRAC MW SOLID

200.00 15.00 0.00 -7.0614 0.0000 0.0032 0.9968

MELTING/FREEZING DATA DUTY NMP COMPONENTS FROZEN FRACTION MM BTU/HR F --------------------- -------- ----------- ------1 UREA 1.0000 -0.2976 270.86

5-36 Urea Plant

March 5, 2014


R PAGE P-21 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci CONVERSION REACTOR SUMMARY Apr_2010 ============================================================================== UNIT 3, 'RX1' OPERATING CONDITIONS REACTOR TYPE ISOTHERMAL REACTOR DUTY, MM BTU/HR -34.7104 TOTAL HEAT OF REACTION AT 77.00 F, MM BTU/HR -38.0197 INLET ----------3 4

FEED LIQUID PRODUCT TEMPERATURE, F PRESSURE, PSIA

OUTLET ----------5 365.00 3515.0000

60.14 3515.0000

REACTION DATA COMPONENT -----------------1 UREA 2 WATER 3 AMCA 4 AMMONIA 5 CO2 TOTAL

--------- RATES, LB-MOL/HR ---------FRACTION FEED CHANGE PRODUCT CONVERTED ----------- ----------- ----------- ----------5.38249E-24 1591.8273 1591.8273 4.33234E-05 1591.8273 1591.8273 1.7863 530.6091 532.3954 9718.5395 -4244.8727 5473.6667 0.4368 2122.4364 -2122.4364 0.0000 1.0000 11842.7622

-2653.0455

LB-MOL/HR BASE COMPONENT REACTION CONVERTED ---------------------------- ----------5 CO2 1 2122.4364 (1) FRACTION CONVERTED BASED ON AMOUNT IN FEED

9189.7167 FRACTION CONVERTED(1) -----------1.0000

REACTOR MASS BALANCE Component -------------------1 UREA 2 WATER 3 AMCA 4 AMMONIA 5 CO2 TOTAL

PRO/II Case Book

----------Feed ----------3.23249E-22 7.80483E-04 139.4570 165512.1650 93408.0000 259059.6228

Rates, LB/HR Change ----------95598.2077 28677.2137 41425.1400 -72292.5579 -93408.0000 0.0000

-----------Fraction Product Converted ----------- ----------95598.2077 28677.2145 41564.5970 93219.6071 0.4368 0.0000 1.0000 259059.6263

Urea Plant 5-37


R PAGE P-22 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci CONVERSION REACTOR SUMMARY Apr_2010 ============================================================================== UNIT 6, 'RX2' OPERATING CONDITIONS REACTOR TYPE ISOTHERMAL REACTOR DUTY, MM BTU/HR 63.1751 TOTAL HEAT OF REACTION AT 77.00 F, MM BTU/HR 32.0677 INLET OUTLET --------------------FEED 8 VAPOR PRODUCT 9 LIQUID PRODUCT 10 TEMPERATURE, F 233.07 302.00 PRESSURE, PSIA 325.0000 325.0000 REACTION DATA COMPONENT -----------------1 UREA 2 WATER 3 AMCA 4 AMMONIA 5 CO2 TOTAL

--------- RATES, LB-MOL/HR ---------FRACTION FEED CHANGE PRODUCT CONVERTED ----------- ----------- ----------- ----------1591.8272 0.0000 1591.8272 1591.8272 0.0000 1591.8272 530.6146 -466.9409 63.6738 0.8800 1922.5107 933.8817 2856.3924 0.0000 466.9409 466.9409 5636.7797 933.8817 6570.6614

LB-MOL/HR BASE COMPONENT REACTION CONVERTED ---------------------------- ----------3 AMCA 1 466.9409 (1) FRACTION CONVERTED BASED ON AMOUNT IN FEED

FRACTION CONVERTED(1) -----------0.8800


5-38 Urea Plant

----------Feed ----------95598.2050 28677.2129 41425.5706 32741.4323 0.0000 198442.4209

Rates, LB/HR Change ----------0.0000 0.0000 -36454.5021 15904.5281 20549.9736

-----------Fraction Product Converted ----------- ----------95598.2050 28677.2129 4971.0685 0.8800 48645.9604 20549.9736

0.0000 198442.4204

March 5, 2014


R PAGE P-23 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci CONVERSION REACTOR SUMMARY Apr_2010 ============================================================================== UNIT 8, 'RX3' OPERATING CONDITIONS REACTOR TYPE ISOTHERMAL REACTOR DUTY, MM BTU/HR 17.7914 TOTAL HEAT OF REACTION AT 77.00 F, MM BTU/HR 1.2566

FEED VAPOR PRODUCT LIQUID PRODUCT TEMPERATURE, F PRESSURE, PSIA

INLET ----------11 158.00 25.0000

OUTLET ----------12 13 252.00 25.0000

REACTION DATA --------- RATES, LB-MOL/HR ---------FRACTION FEED CHANGE PRODUCT CONVERTED ----------- ----------- ----------- ----------1591.7928 0.0000 1591.7928 1385.2013 0.0000 1385.2013 18.3068 -18.2977 9.15342E-03 0.9995 619.4463 36.5954 656.0417 23.1057 18.2977 41.4034 3637.8529 36.5954 3674.4483 LB-MOL/HR FRACTION BASE COMPONENT REACTION CONVERTED CONVERTED(1) ---------------------------- ---------------------3 AMCA 1 18.2977 0.9995 (1) FRACTION CONVERTED BASED ON AMOUNT IN FEED COMPONENT -----------------1 UREA 2 WATER 3 AMCA 4 AMMONIA 5 CO2 TOTAL


PRO/II Case Book

----------- Rates, LB/HR -----------Fraction Feed Change Product Converted ----------- ----------- ----------- ----------95596.1349 0.0000 95596.1349 24954.7892 0.0000 24954.7892 1429.2311 -1428.5165 0.7146 0.9995 10549.5170 623.2394 11172.7564 1016.8772 805.2771 1822.1543 133546.5494

0.0000 133546.5494

Urea Plant 5-39


R PAGE P-24 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci STREAM WEIGHT COMPONENT RATES Apr_2010 ============================================================================== STREAM ID NAME PHASE THERMO ID FLUID 1 2 3 4 5 6 7 8 TOTAL

RATES, LB/HR UREA WATER AMCA AMMONIA CO2 N2 O2 H2 FLUID, LB/HR

MW SOLID RATES, LB/HR 1 UREA 2 WATER 3 AMCA 4 AMMONIA 5 CO2 6 N2 7 O2 TOTAL MW SOLID, LB/HR TOTAL RATE, LB/HR TEMPERATURE, F PRESSURE, PSIA ENTHALPY, MM BTU/HR MOLECULAR WEIGHT WEIGHT FRAC VAPOR WEIGHT FRAC LIQUID WEIGHT FRAC MW SOLID

5-40 Urea Plant

1 NH3FD LIQUID NRTL01 0.0000 0.0000 0.0000 105049.0000 0.0000 0.0000 0.0000 0.0000 105049.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 105049.0000 -28.0000 320.0000 -6.7624 17.0306 0.0000 1.0000 0.0000

2 CO2FD VAPOR NRTL01

3

4

LIQUID NRTL01

LIQUID NRTL01

0.0000 0.0000 0.0000 7.8048E-04 0.0000 139.4570 0.0000 165512.1650 93408.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 93408.0000 165651.6228

0.0000 0.0000 0.0000 0.0000 93408.0000 0.0000 0.0000 0.0000 93408.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

93408.0000 165651.6228

93408.0000

100.0000 300.0000 4.7133 44.0098 1.0000 0.0000 0.0000

44.6511 3515.0000 2.2745 17.0418 0.0000 1.0000 0.0000

100.0000 3515.0000 4.7133 44.0098 0.0000 1.0000 0.0000

March 5, 2014





PRO/II Case Book

5

6

7

8

LIQUID NRTL01

MIXED NRTL01

LIQUID NRTL01

LIQUID NRTL01

95598.2077 95598.2077 28677.2145 28677.2145 41564.5970 41564.5970 93219.6071 93219.6071 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 259059.6263 259059.6263 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

259059.6263 259059.6263 365.0000 3515.0000 77.4783 28.1902 0.0000 1.0000 0.0000

292.4821 320.0000 77.4783 28.1902 0.4585 0.5415 0.0000

0.0000 95598.2050 7.7806E-04 28677.2129 139.0253 41425.5706 60478.1766 32741.4323 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 60617.2026 198442.4209 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

60617.2026 198442.4209 127.9653 320.0000 6.5832 17.0612 0.0000 1.0000 0.0000

233.0678 325.0000 26.9806 35.2049 0.0000 1.0000 0.0000

Urea Plant 5-41





5-42 Urea Plant

9 DECGS1 VAPOR NRTL01

10

11

LIQUID NRTL01

MIXED NRTL01

12 DECGS2 VAPOR NRTL01

2.0701 95596.1349 95596.1349 3722.4238 24954.7892 24954.7892 3541.8374 1429.2311 1429.2311 38096.4434 10549.5170 10549.5170 19533.0964 1016.8772 1016.8772 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 64895.8710 133546.5494 133546.5494

2.4577 8909.5732 0.6093 10493.9902 1802.8394 0.0000 0.0000 0.0000 21209.4698

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

64895.8710 133546.5494 133546.5494

21209.4698

302.0000 325.0000 25.0732 22.1276 1.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

302.0000 325.0000 24.0578 36.7103 0.0000 1.0000 0.0000

158.0000 25.0000 13.5648 36.7103 0.0565 0.9435 0.0000

252.0000 25.0000 15.9134 18.4149 1.0000 0.0000 0.0000

March 5, 2014





PRO/II Case Book

13 LIQUID NRTL01 95593.6772 16045.2159 0.1053 678.7662 19.3149 0.0000 0.0000 0.0000 112337.0796 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 112337.0796 252.0000 25.0000 13.8352 44.5306 0.0000 1.0000 0.0000

14 FLGS1 VAPOR NRTL01

LIQUID NRTL01

16 FLGS2 VAPOR NRTL01

0.2755 95593.4017 989.5365 15055.6794 0.0422 0.0632 441.1092 237.6570 17.7209 1.5940 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 1448.6843 110888.3952

0.0973 512.6611 0.0153 127.4104 1.4026 0.0000 0.0000 0.0000 641.5867

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

15

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

1448.6843 110888.3952

641.5867

250.0000 15.0000 1.3812 17.8329 1.0000 0.0000 0.0000

250.0000 15.0000 13.3529 45.4190 0.0000 1.0000 0.0000

230.0000 8.7834 0.6619 17.8357 1.0000 0.0000 0.0000

Urea Plant 5-43





5-44 Urea Plant

17

18 LIQUID NRTL01

19 CRYGS1 VAPOR NRTL01

LIQUID NRTL01

MIXED NRTL01

95593.3044 95593.3044 14543.0183 14543.0183 0.0479 0.0479 110.2466 110.2466 0.1914 0.1914 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 110246.8085 110246.8085

3.6000E-03 629.8924 9.0884E-03 78.2450 0.1862 0.0000 0.0000 0.0000 708.3363

31298.5069 13913.1259 0.0388 32.0015 5.2651E-03 0.0000 0.0000 0.0000 45243.6784

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

64294.7938 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 64294.7938

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

110246.8085 110246.8085 230.0000 8.7834 11.9853 45.8314 0.0000 1.0000 0.0000

230.0511 20.0000 11.9884 45.8314 0.0000 1.0000 0.0000

20

708.3363 109538.4722 130.0000 1.5000 0.7478 17.9039 1.0000 0.0000 0.0000

130.0000 1.5000 -0.6767 46.2984 0.0000 0.4130 0.5870

March 5, 2014





PRO/II Case Book

21

22

23

MIXED NRTL01

LIQUID NRTL01

MIXED NRTL01

24 CRYGS2 VAPOR NRTL01

31298.5069 13913.1259 0.0388 32.0015 5.2651E-03 0.0000 0.0000 0.0000 45243.6784

29069.4643 12922.2495 0.0360 29.7224 4.8901E-03 0.0000 0.0000 0.0000 42021.4772

2229.0426 990.8763 2.7628E-03 2.2791 3.7497E-04 0.0000 0.0000 0.0000 3222.2012

0.0399 7003.5393 0.0310 29.2626 4.8848E-03 0.0000 0.0000 0.0000 7032.8776

64294.7938 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 64294.7938

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

64294.7938 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 64294.7938

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

109538.4722

42021.4772

67516.9950

7032.8776

130.0609 20.0000 -0.6734 46.2984 0.0000 0.4130 0.5870

130.0609 20.0000 2.6376 34.9282 0.0000 1.0000 0.0000

130.0609 20.0000 -3.3109 58.0622 0.0000 0.0477 0.9523

130.0000 1.3350 7.8496 18.0111 1.0000 0.0000 0.0000

Urea Plant 5-45


R PAGE P-30 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci STREAM WEIGHT COMPONENT RATES Apr_2010 ============================================================================== STREAM ID NAME PHASE THERMO ID

25

26

27

28

MIXED NRTL01

MIXED NRTL01

LIQUID NRTL01

MIXED NRTL01

13305.9443 5918.7102 5.0685E-03 0.4598 5.2985E-06 0.0000 0.0000 0.0000 19225.1195

13305.9443 5918.7102 5.0685E-03 0.4598 5.2985E-06 0.0000 0.0000 0.0000 19225.1195

12709.6529 5653.4697 4.8413E-03 0.4392 5.0611E-06 0.0000 0.0000 0.0000 18363.5667

596.2914 265.2405 2.2714E-04 0.0206 2.3745E-07 0.0000 0.0000 0.0000 861.5528

MW SOLID RATES, LB/HR 1 UREA 2 WATER 3 AMCA 4 AMMONIA 5 CO2 6 N2 7 O2 TOTAL MW SOLID, LB/HR

15763.4801 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 15763.4801

15763.4801 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 15763.4801

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

15763.4801 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 15763.4801

TOTAL RATE, LB/HR

34988.5996

34988.5996

18363.5667

16625.0329

130.0000 1.3350 0.3437 43.0572 0.0000 0.5495 0.4505

130.0768 20.0000 0.3451 43.0572 0.0000 0.5495 0.4505

130.0768 20.0000 1.1523 34.9468 0.0000 1.0000 0.0000

130.0768 20.0000 -0.8072 57.8998 0.0000 0.0518 0.9482

FLUID 1 2 3 4 5 6 7 8 TOTAL


TEMPERATURE, F PRESSURE, PSIA ENTHALPY, MM BTU/HR MOLECULAR WEIGHT WEIGHT FRAC VAPOR WEIGHT FRAC LIQUID WEIGHT FRAC MW SOLID

5-46 Urea Plant

March 5, 2014





PRO/II Case Book

29 DRYGS VAPOR NRTL01

30 MIXED NRTL01

31 UREAPROD MIXED NRTL01

14.6664 1176.0587 2.9791E-03 2.2917 3.7480E-04 0.0000 0.0000 0.0000 1193.0202

2810.6676 80.0582 1.0834E-05 7.9784E-03 4.1472E-07 0.0000 0.0000 0.0000 2890.7338

0.0000 80.0582 1.0834E-05 7.9784E-03 4.1472E-07 0.0000 0.0000 0.0000 80.0662

0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

80058.2739 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 80058.2739

82868.9415 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 82868.9415

1193.0202

82949.0077

82949.0077

369.5322 15.0000 1.4214 18.1697 1.0000 0.0000 0.0000

369.5322 15.0000 5.0183 59.9207 0.0000 0.0348 0.9652

200.0000 15.0000 -2.0431 59.9207 0.0000 9.6525E-04 0.9990

Urea Plant 5-47


R PAGE P-32 PRO/II VERSION 9.3 ELEC V7.0 OUTPUT SimSci SOLID ATTRIBUTES Apr_2010 ============================================================================== STREAM ID NAME PHASE THERMO ID 1

UREA PSD, MIC 0.000 20.00 50.00 100.0 200.0 0.500 -

STREAM ID NAME PHASE THERMO ID 1

UREA PSD, MIC 0.000 20.00 50.00 100.0 200.0 0.500 -

5-48 Urea Plant

20

21

23

25

MIXED NRTL01

MIXED NRTL01

MIXED NRTL01

MIXED NRTL01

20.00 1.422E-06 50.00 8.265E-05 100.0 1.153E-03 200.0 0.0136 500.0 0.2314 1.000 E+03 0.7537

1.422E-06 8.265E-05 1.153E-03 0.0136 0.2314 0.7537

1.422E-06 8.265E-05 1.153E-03 0.0136 0.2314 0.7537

4.925E-06 2.719E-04 3.492E-03 0.0353 0.3966 0.5643

26

28

30

MIXED NRTL01

MIXED NRTL01

MIXED NRTL01

31 UREAPROD MIXED NRTL01

20.00 4.925E-06 50.00 2.719E-04 100.0 3.492E-03 200.0 0.0353 500.0 0.3966 1.000 E+03 0.5643

4.925E-06 2.719E-04 3.492E-03 0.0353 0.3966 0.5643

2.112E-06 1.199E-04 1.614E-03 0.0179 0.2639 0.7164

2.112E-06 1.199E-04 1.614E-03 0.0179 0.2639 0.7164

March 5, 2014

Invensys Systems, Inc. 26561 Rancho Parkway South Lake Forest, CA 92630 United States of America http://iom.invensys.com

Global Customer Support Inside U.S.: 1-866-746-6477 Outside U.S.: 1-508-549-2424 or contact your local Invensys Representative. Email: [email protected] Website: http://support.ips.invensys.com

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