Open Access

Department of Chemical and Environmental Engineering, Master of Science in Environmental Engineering, the University of Arizona, USA

- *Corresponding Author:
- David Jonathas

Department of Chemical and Environmental Engineering

Master of Science in Environmental Engineering

The University of Arizona

USA

**Tel:**+15202455391

**E-mail:**johndave2009@gmail.com

**Accepted date:** January 19, 2017

**Citation:** Jonathas D. Modeling of Nucleation Rate of Supersaturated Calcium Sulfate Solutions. Environ Risk Assess Remediat. 2017;1(1):30-39

Reverse osmosis treatment of the Central Arizona Project (CAP) water provokes scaling because of its high content in salt. Experiments simulating various solutions of calcium sulfate (CaSO4) made by mixing of sodium sulfate (Na2SO4) and calcium chloride (CaCl2) reinforced this idea. An increase of the degree of supersaturation of the solution from 8.67 to 42.08 decreased the induction time for precipitation of calcium sulfate solutions. The use of Flocon® 135 as antiscalant increased the induction time. The increase was directly related to the concentration of antiscalant. Working with 11.06 degree of supersaturation, a dose 0 ppm of antiscalant has an induction time of 217 minutes. A dose of 0.5 ppm of Flocon 135 inhibits completely the crystal growth in solution. The use of 21.07 degree of supersaturation showed an induction time of 36 minutes for 0 ppm of antiscalant, 78 minutes for 0.25 ppm of antiscalant, 91 minutes for 0.5 ppm of antiscalant, 119 minutes for 0.75 ppm of antiscalant, 139 minutes for 1 ppm of antiscalant, 243 minutes for 1.25 ppm of antiscalant, and crystal growth and nucleation rate are completely inhibited by use from 2 ppm or more of antiscalant. The use of a solution of 42.08 degree of supersaturation gave the following results: 11 minutes to nucleation for 0 ppm of antiscalant, 19 minutes for 0.5 ppm of antiscalant, 24 minutes for 1 ppm of antiscalant, 36 minutes for 1.5 ppm of antiscalant, 84 minutes for 2 ppm of antiscalant, and 123 minutes for 2.5 ppm of antiscalant. The nucleation rate was 2.1 × 109 nuclei/cm3.min for 8.67 degree of supersaturation to 1.26 × 1027 nuclei/cm3.min for 42.06 degree of supersaturation. Logarithmic plots of the induction time (tind ) as function of 1/[ln(S)]2 for calcium sulfate without and with addition of antiscalant for fixed temperature provides a linear trend with slope B as a constant proportional to the surface tension and molar volume. Modeling of the nucleation rate allows predicting the induction time by knowing a unique constant value (C=22.86) associated to each nucleation rate (from 5.05 × 1011 to 1.22 × 1028). Each nucleation rate values are related to a specific degree of supersaturation (from 8.67 to 42.06) by this equation:

Nucleation, Supersaturated.

Arizona has a desert climate and water is a big issue here. About
2.5 million acre-feet of groundwater are mined each year in the
state in order to satisfy demand. Without any long-term solution,
there are risks of serious structural damage to homes, agricultural
lands and industry from groundwater overdraft. The Central
Arizona Project (CAP) project was authorized to counteract the
overdraft by providing an alternative source of surface water.
The canal is 336 miles extending from Lake Havasu City to
the Tucson Active Management Area (TAMA). Water demand
in the TAMA is about 400,000 AFY. It is satisfied through
contradictory natural groundwater replenishment (15%) CAP
deliveries (60%) and incidental reused of water (**Figure 1**).

The CAP water has a high concentration in total dissolved
solids (**Table 1**). A straight forward mass balance indicts that
CAP water brings about 200,000 metric tons of salt into the
TAMA each year. Without any salt management program, there will be an increase of about 5 mg/L-year of salt in the regional
aquifer. The salt content of the aquifer will double over the next
50 years. Reverse osmosis (RO) is used to separate salt from
water. Water is forced through a semi-permeable membrane
under sufficient pressure to overcome osmotic pressure of the
feed water source. Required pressure depends on feed water
salinity, the fraction of water recovered and the membrane type
itself. Recovery is the percentage of influent water recovered as
reverse osmosis permeates. Scaling problems during the reverse
osmosis process decrease the percentage of recovery, lead to
higher pressure requirements and reduce the permeability of the
membrane. Scaling problems during reverse osmosis process
can be avoided by use of antiscalant.

Precipitate | Ion Concentration | Log (ion product) | log K_{so} |
Degree of Saturation(b) |
---|---|---|---|---|

BaSO_{4}(s) |
[Ba^{+2}]=1.17 × 10^{-6}M[SO _{4}^{-2}]=2.81 × 10^{-3}M |
-8.48 | -10.0 | 827.83 |

CaSO_{4}(s) |
[Ca^{+2}]=2.0 × 10^{-3}M |
-5.25 | -4.85 | 9.95 |

CaCO_{3}(s) |
[CO_{3-2}]=1.0 × 10^{-3} M(a) |
-7.7 | -8.48 | 150.64 |

**Table 1.** Concentration and solubility data for CAP water species that may contribute to membrane scaling [1].

Chemical composition of many known antiscalant is not welldefined by the manufacturer. So, their rational selection for membrane separations is difficult. The need of direct antiscalant testing on the water to be treated is more than necessary [2].

Understanding the effect of amino trismethylenephosphonic
acid (ATMP) on calcium sulfate dehydrate (gypsum) was
accrued out (**Table 2**) [3]. Mahmoud et al. [4] studied the effect of
surfactants on the crystallization of gypsum under conditions of
the simulated dehydrate process of phosphoric acid production.
Experimental determination of antiscalant effectiveness has
been limited to quantification of scaling behavior based on
flux decline measurements or determining the extent of surface
area coverage by mineral scale [5]. However, efforts to date
have not yield quantitative information regarding the impact
of antiscalants on mineral crystal nucleation rate. Investigation
of the nucleation rate without and with addition of antiscalant
should give a more fundamental and means of prediction of the
induction time [6].

Water Quality Constituent (mg/L) | Tucson Water Production Wells | CAP Water |
---|---|---|

Total Dissolved Solids | 259 | 666 |

Hardness (as CaCO_{3}) |
119 | 270 |

Sodium | 40 | 112 |

Chloride | 17 | 104 |

Calcium | 39 | 56 |

Magnesium | 5 | 31 |

Sulfate | 45 | 280 |

Alkalinity (as CaCO_{3}) |
126 | 98 |

TOC | <1 | 3.5 |

**Table 2.** Water quality comparison between Tucson groundwater and
CAP water.

**The experiment**

The basis of the experiment is to determine the induction time for precipitation of calcium sulfate in solution using a jar tester. Different degrees of supersaturation of the solution are used based on the activities of calcium and sulfate ions present in solution. Addition of antiscalant and the impact on the induction time for precipitation of calcium sulfate where studied as well.

**Preparation of CaCl _{2}·2H_{2}O and Na_{2}SO_{4} solutions**

One molar calcium chloride solution was prepared by diluting
147.02 grams of CaCl_{2}.2H_{2}O in one liter of distilled water. A volumetric flask of 1 liter was used to prepare the solution. Also,
one molar sodium sulfate was prepared by adding 111 grams of
Na_{2}SO_{4} to a liter of water. A volumetric flask of 1 liter was used
again to dissolve the chemical. These were stock solutions for
the experiments that followed.

**Preparation of 5 g/L antiscalant stock solution**

Flocon® 135 is a pure antiscalant in liquid form. Its impact on induction time was evaluated here. Five grams of pure liquid antiscalant was added to 1 liter volumetric flask and diluted with deionized water a final volume of 1 liter. Calculation was made to end up to 0.25 ppm until 4 ppm concentration of antiscalant to use.

About 1 mL was taken from the 1 L stock solution of antiscalant and put in a 100 mL volumetric flask and completed with DI water. The new concentration was then 50 mg/L from this calculation:

C_{1}V_{1}=C_{2}V_{2}

(5 g/L) × (1 mL)=C_{2} × (100 mL)

C_{2}=50 mg/L

So, to know the volume to take from the 1 L stock solution of antiscalant and to end up to 0.5 ppm (0.5 mg/L) concentration of antiscalant, this calculation was made:

C_{1}V_{1}=C_{2}V_{2}

(50 mg/L) × (V_{1})=(0.5 mg/L) × (1 L)

V_{1}=10 mL

**Preparation of supersaturated CaSO _{4} solution**

To prepare a solution with a degree of supersaturation of 31.7,
the followed were carried out. About 92 mL from the 1 liter of
stock solution of Na_{2}SO_{4} was transferred to a 500 mL volumetric
flask. Water was added to the volumetric flask to reach a final
volume of 500 mL. The same procedure was followed with
CaCl_{2}·2H_{2}O.

**Mixing of prepared solutions**

A beaker of 2 liter capacity was used to mix the two solutions
which was 1 liter total. The sodium sulfate solution was
added first to the beaker. And then, the calcium sulfate was
poured in the calcium sulfate solution in the beaker. Reactors
were duplicated in parallels in each experiment to establish
reproducibility (**Figure 2**).

**Data measurement**

Two solutions in the beaker marked the beginning of each
experiment. Time after mixing was monitored and recorded.
The solution-stirring was performed at constant speed using
a jar tester with mechanic stirrers. Other author used instead
to steer the solution magnetic stirrer at constant speed [7]. A
dual-path spectrophotometer (Shimadzu UV-160A) was used to
record the time-dependent absorbance of the stirred solutions
(**Figure 3**). The spectrophotometer was zeroed with distilled
water. The wavelength used for the measurement was 600 nm.
Absorbances of samples were measured against distilled water.
Each 5 minutes 2-3 ml of CaSO_{4} solution were withdrawn for
absorbance measurements.

**Determination of the degree of supersaturation of
calcium sulfate**

Defined volumes of sodium sulfate and calcium chloride were withdrawn from the 1 molar stock solution to produce specific
degrees of supersaturation of calcium sulfate after mixing (**Table
3**). The calculation provided illustrates details for preparing a
solution of 31.7 degree of supersaturation of calcium sulfate
(**Figure 4**).

21.07 degree of supersaturation of calcium sulfate with 0 ppm antiscalant | |||
---|---|---|---|

Test 1 | Test 2 | ||

Time (min) | Absorbance | Time (min) | Absorbance |

1 | 0.068 | 2 | 0.07 |

6 | 0.054 | 7 | 0.08 |

12 | 0.083 | 14 | 0.063 |

19 | 0.058 | 20 | 0.063 |

25 | 0.061 | 26 | 0.064 |

29 | 0.064 | 32 | 0.072 |

32 | 0.07 | 34 | 0.071 |

39 | 0.077 | 40 | 0.075 |

47 | 0.095 | 49 | 0.096 |

55 | 0.117 | 56 | 0.118 |

58 | 0.14 | 59 | 0.15 |

69 | 0.276 | 70 | 0.229 |

74 | 0.382 | 76 | 0.283 |

77 | 0.44 | 77 | 0.359 |

83 | 0.635 | 84 | 0.5 |

96 | 0.803 | 97 | 0.688 |

116 | 0.988 | 116 | 0.99 |

134 | 1.146 | 135 | 1.1 |

**Table 3.** Data of the 21.07 degree of supersaturation of calcium sulfate
with 0 ppm of antiscalant.

**Calculation for Na _{2}SO_{4}**

V_{1} * C_{1}=V_{2} * C_{2}

C_{1}=142 g/L

V_{1}=92 mL

V_{2}=500 mL

C_{2}=26.13 g/L

SO_{4} 2-=0.092 mol

**Calculation for CaCl _{2}**

V_{1} * C_{1}=V_{2} * C_{2}

C_{1}=111 g/L

V_{1}=92 mL

V_{2}=500 mL

C_{2}=20.42 g/L

Ca^{2+}=0.092 mol

I=0.276+0.276

I = 0.552

S = 31.7

I: Ionic strength

Ƴ: activity coefficient

S: supersaturation of a solution

**Determination of the induction time of precipitation of
calcium sulfate**

The bold data was used to calculate the average ÿ value which served to determine the induction time.

The induction time was determined by calculation using each
of the graphs presented. Data from the flat part of the graph
before precipitation reactions were evident are used to calculate
an average value of ÿ. Five times the standard deviation (σ) was
added to the average data of the flat part of the curve. Following
the onset of precipitation, solution absorbance values generally
increased exponentially for at least a few minutes (**Table 4**). The
induction time for each experiment was arbitrarily calculated
from: after m, k and σ were determined
experimentally. A t_{ind} value was determined in this manner from
each experiment. Values showed in summary tables and figures
are the average y duplicate experiments in parallels.

21.07 supersaturated calcium sulfate with 0 ppm of antiscalant | |||
---|---|---|---|

Test 1 | Test 2 | ||

Time (min) | Absorbance | Time (min) | Absorbance |

1 | 0.068 | 2 | 0.07 |

6 | 0.054 | 7 | 0.08 |

12 | 0.083 | 14 | 0.063 |

19 | 0.058 | 20 | 0.063 |

25 | 0.061 | 26 | 0.064 |

29 | 0.064 | 32 | 0.072 |

32 | 0.07 | 34 | 0.071 |

39 | 0.077 | 40 | 0.075 |

Average (ÿ) | 0.066875 | Average (ÿ) | 0.06975 |

Standard deviation (σ) | 0.009717 | Standard deviation (σ) | 0.006135 |

y value (y=ÿ+5*σ) | 0.194607 | y value (y=ÿ+5*σ) | 0.168833 |

y=0.0089 | y=0.0117 | ||

0.194607=0.0089 | 0.168833=0.0117 | ||

x=61 | x=62 |

**Table 4.** Methodology to calculate the induction time of the 21.07
degree of supersaturation of calcium sulfate with 0 ppm of antiscalant.

**Determination of the nucleation rate of calcium sulfate**

The nucleation rate of calcium sulfate was calculated using equation 9 plotted in Excel. Most of the parameters used (pre-exponential value, surface tension, molar volume, Boltzmann constant, temperature) are constant and their value was plotted. The other values (degree of supersaturation and induction time) were determined by some methods explained earlier.

Various degrees of supersaturation of calcium sulfate without addition of antiscalant

Experiments were conducted with various degrees of supersaturation of calcium sulfate without addition of antiscalant. Those data show a decrease of the measured induction time when the degree of supersaturation increases. Crystal growth increases in a trend related to the degree of supersaturation. Scaling occurs faster during RO process when the salt concentration in the water is higher. Results from [8-10] experiments shown an increase of the degree of supersaturation of calcium sulfate when the Gibbs free energy change needed for the formation of critical nucleus size decreased.

Various degrees of supersaturation of calcium sulfate with addition of antiscalant

Experiments were also conducted with various degrees of
supersaturation of calcium sulfate with addition of antiscalant.
The results are combined in (**Figure 5**).

Various degrees of supersaturation of calcium sulfate in increase
level are plotted versus the induction time in minutes. We see
a gradual tendency for the graphs to go far to the right which
correspond to higher induction time. This mean the induction
time increases with a decrease of the degree of supersaturation
[11]. That means during Reverse osmosis operation lower
concentration of salt in the feed water is favorable to the
treatment. And in case of increase of salt in the feed water like
in the case of a brackish water an inhibition is needed like an
antiscalant to push the system in the reverse mode of what it
will intend to do. An antiscalant would increase the induction
time by now allowing particles of salt like calcium sulfate to
stick together and form bigger particles (**Figure 6**). Modeling of
the addition of antiscalant in various supersaturated solutions of
calcium sulfate.

We are trying to find a model which can fit the relation between the concentration of antiscalant use to delay the salt deposit (induction time) during reverse osmosis process (RO) to get clean water. Modeling of the result can open broad perspective for the results [12].

We were able to find an equation in the form: y=Ax^{B}

with x: amount of antiscalant (ppm)

y: induction time (minutes)

This equation was picked because it can fit our data.

We can then write the equation in this form:

(21)

which is related to the affine equation: y=mx+b

(22)

Equation (22) fit the results of the close relation between
induction time and amount of antiscalant (**Figure 7**) use during
RO process. The result seems to support our conclusions of an increase of the amount of antiscalant impact.

We can finalize the calculation and

We ended up with: log (A)=2.2752 and Blog(x)=0.8623log(x)

After calculation: A=188.45

and B=0.8623

So, the equation of the progressive addition of antiscalant in the 21.07 degree of supersaturation of calcium sulfate which has an impact on the induction time is:

Y=188.45x^{0.8623} (23)

log(y)=1.1659 log(x) + 1.512 (14)

log (A)=1.512 and Blog(x)=1.1659log(x)

A=32.51

B=1.1659

y=32.51x^{1.1659} (24) (**Figure 8**)

From all those figures above, it can be concluded that progressive
addition of antiscalant delayed the crystal growth and the
nucleation rate. Measurement of the induction time shows
delays. And more addition of antiscalant provokes complete
inhibition of precipitation of calcium sulfate. A form of y=Ax^{B} curve was used to model the amount of antiscalant added (x)
and the measured induction time related (y) [13]. Logarithmic
plots of the induction time versus degree of supersaturation of
calcium sulfate solutions with different addition of antiscalant
shows linear curves (**Figure 9**) with a gradual decrease of the
slope.

**Predicted nucleation rate and induction time of supersaturated
calcium sulfate solutions at room temperature**

The nucleation rate equation allowed calculating the nucleation
of various degree of supersaturated solution of calcium sulfate.
The temperature was maintained constant at room temperature.
It has been proved that the nucleation rate is controlled by three
factors: supersaturation, temperature and interfacial tension
[7]. The nucleation rate (nuclei/m^{3}.min), the number of nuclei
formed per unit time per volume has been calculated as follow
(equation 19):

**Figure 10** for a constant saturation level and temperature, the
interfacial tension has a strong impact on the nucleation process.
During the crystal growth, the solution becomes more stable
while the degree of supersaturation decrease gradually until
the solution reach equilibrium. Equilibrium of the solution is
presented by the flat part of the graphs. The experiments showed
that increase of the degree of supersaturation of calcium sulfate
solutions in water medium decrease the induction time. Increase
addition of antiscalant (Flocon 135) delays progressively
the induction time until any precipitation occurs. Söhnel and
Mullin [14] established a relationship between induction time
and nucleation rate stating that

(25)

(26)

(27)

(28)

(29) as slope

σ: surface energy (4.26 × 10^{-2} J/m2)

ν: molar volume (7.47 × 10-5 m^{3}/mol)

k: Boltzmann constant (1.3806503 × 10^{-23} J/K)

T: absolute temperature (Kelvin)

S: degree of supersaturation of the water

A: pre-exponential factor (1036 nuclei/m^{3} × min)

Jn: Nucleation rate (nuclei/m^{3} × min)

B: Constant

The induction time helps to evaluate the effect of supersaturation,
temperature, organic or mineral additives on calcium sulfate
crystallization. Based on the classic homogeneous nucleation
theory, the induction time is related to the supersaturation
(**Table 5**). Logarithmic plot of t_{ind} as function of 1/(ln S)^{2} for
fixed temperature gives straight line with slope B [7]. A change
in the slope of the linearization of experimental results may
indicate a transition from homogeneous to heterogeneous
nucleation mechanisms.

ppm of antiscalant | S | Jn | t_{ind} |
ln (S) | (ln S)^{2} |
1/(ln S)^{2} |
ln (t_{ind}) |
---|---|---|---|---|---|---|---|

0 | 8.67 | 2.10E+09 | 264 | 2.159869 | 4.66503319 | 0.21436075 | 5.575949103 |

0 | 9.4 | 1.63E+11 | 197 | 2.24071 | 5.02077991 | 0.19917224 | 5.283203729 |

0 | 11.06 | 2.85E+14 | 150 | 2.403335 | 5.7760191 | 0.17312962 | 5.010635294 |

0 | 14.79 | 7.11E+18 | 141 | 2.693951 | 7.25737348 | 0.1377909 | 4.94875989 |

0 | 21.07 | 4.02E+22 | 36 | 3.04785 | 9.28939101 | 0.10764968 | 3.583518938 |

0 | 25.29 | 1.19E+24 | 25 | 3.230409 | 10.4355427 | 0.09582635 | 3.218875825 |

0 | 31.7 | 3.83E+25 | 16 | 3.456317 | 11.946125 | 0.08370915 | 2.772588722 |

0 | 37.45 | 3.31E+26 | 8 | 3.623007 | 13.1261776 | 0.07618364 | 2.079441542 |

0 | 42.08 | 1.26E+27 | 10 | 3.739573 | 13.984403 | 0.07150824 | 2.302585093 |

**Table 5.** Nucleation rate of supersaturation of solutions of calcium sulfate without addition of antiscalant.

The calculated slope (B=287) differs from linear curve slope (23.538) by a factor of 10. It can indicate that there is a passage from homogeneous to heterogeneous nucleation.

Alimi [15] got similar results when plotting the log of the
induction time versus various degree of supersaturation of
calcium sulfate dihydrate for temperatures ranging between
20ºC and 70ºC (**Figure 11**). In the case of our study, the
temperature was maintained constant. It seems that at high
temperature, Prisciandaro [16] recorded also a passage of the
slopes from homogeneous to heterogeneous nucleation which is
consistent to results [15].

The induction time can be predicted base on values of the
surface tension (σ), molar volume (ν), Boltzmann constant
(k), room temperature (298 K), degree of supersaturation (S),
pre-exponential factor (A). Value of the slope was calculated
(**Figure 12**). This value (B) was then used to get the C value
from equation (28).

**Figure 12.** log (t_{ind})=f [(log S)^{2}] for different temperature levels [15].

(28)

we know that Cʹ=C/A

(30)

supersaturation of calcium sulfate solutions gives a linear curve related to this equation:

23.538x + 0.7915 (31)

So, we can conclude that :

(32)

C =10.36e^{0.7915} (33)

we know that A=10^{36} nuclei/m^{3}.min

C =10.36e^{0.7915} (34)

C=22.86 (35)

The C value is then used in this equation:

(25)

(35)

The induction time can be predicted by knowing the nucleation rate using equation (35). This result fit the model (equation 28).

Slopes of the logarithmic plots of the induction time versus
degree of supersaturation of calcium sulfate solutions with
different addition of antiscalant is associated to each dose of
antiscalant (**Table 6**). A linear curve shows that those slopes
increase gradually with the addition of antiscalant (**Figure 13**).
The slope of the Logarithmic plot of the induction time versus
degree of supersaturation of calcium sulfate solutions (equation
31) is equal to the linear curve.

Slope of the antiscalant equation | Dose of antiscalant (ppm) |
---|---|

23.674 | 0 |

41.423 | 0.5 |

45.755 | 1 |

53.628 | 1.25 |

**Table 6.** Relation between slopes of figure 30 and addition of antiscalant.

y = 23.538x + 0.7915 (31)

y = 22.152x + 25.89 (36)

The Tucson Active management Area (TAMA) is relying on
the CAP water to satisfy 50% of the 400,000 AFY. This has
strong consequences for the quality of the delivered water and
concentrations of total dissolved solids (TDS). Membrane
treatment via reverse osmosis process is most commonly used
for separating salt from fresh water. During the process salt
accumulates on the surface membrane and scaling occurring. The
surface blockage of the scale results in permeate flux decline,
reducing the efficiency of the process and increasing operating
costs. Surface tension, temperature of the solution and the degree
of supersaturation of the solution are key factors for crystal growth
and nucleation rate. The use of antiscalant allows inhibition of
the crystal growth in the feed water during the reverse osmosis
process. Antiscalants are mixtures of various molecular weights of
polycarboxylates and polyacrylates. The induction time, elapsed
time between the onset of the supersaturation and the formation
of the first critical nucleus, is delayed by addition of antiscalant.
An increase of the degree of supersaturation of the solution
decreases the induction time while an increase in the amount of
antiscalant add in the feed water increases the induction time. A
linear regression type was found between logarithmic values of
the degree of supersaturation and the induction time without and
with addition of antiscalant. The induction time is proportional to
the inverse of the nucleation by a constant value named C. Each
degree of supersaturation (S) is associated to a nucleation rate
which is related to a C value. So, by knowing the C value for each
degree of supersaturation (S) of calcium sulfate solutions, the
induction time (t_{ind}) can be predicted. Calculation showed that the
measured induction time is very close to the predicted induction
time. Methods for increasing water recovery during salt removal
can involve post-treatment of the brine deriving from the reverse
osmosis process. The Vibratory Separation Enhanced Process
(VSEP). VSEP system includes intense sheer waves, solids and
foulants lifted off on the face of the membrane. Recovery by use
of a combination of RO and VSEP treatments are in the range of
95-99%.

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