Control of the direct hydration process of propylene in accordance with its dynamics Текст научной статьи по специальности «Электротехника, электронная техника, информационные технологии»

ISSN 2522-1841 (Online) ISSN 0005-2531 (Print)

AZERBAIJAN CHEMICAL JOURNAL № 3 2019

15

UDC 66.012/663.5:661.725.3

CONTROL OF THE DIRECT HYDRATION PROCESS OF PROPYLENE IN ACCORDANCE WITH ITS DYNAMICS

A.M.Aliyev, A.R.Safarov, I.V.Balayev, A.M.Guseynova, R.Y.Agayeva, F.G.Bayramov*

M.Nagiyev Institute of Catalysis and Inorganic Chemistry, NAS of Azerbaijan * Azerbaijan State Oil and Industry University

[email protected]

Received 05.03.2019

The article offers calculation of the hydration process proceeding under non-stationing conditions, caused by the removal of phosphoric acid from the carrier and leading to a decrease in the productivity of isopropyl alcohol. For maintaining the stable operation of the catalyst the control function has been proposed of which taking into account in the mathematical model of the process allows keeping the productivity of isopropyl alcohol at the constant level.

Keywords: hydration, propylene, isopropyl alcohol, addition of phosphoric acid control.

https://doi.org/10.32737/0005-2531-2019-3-15-19

Problem statement

Isopropanol is one of the large-scale and widely used products of organic synthesis. It is a good, although flammable, solvent; widely used in medicine as an antiseptic; the substance is indispensable in the processing of petroleum, in pharmacology, also in cosmetology, in the chemical and furniture industry. It is used to synthesize acetone, hydrogen peroxide, iso-propylamine, isopropyl acetate, surfactants and some pharmaceutical preparations.

Isopropanol is currently produced by direct hydration of propylene. The catalyst for the direct hydration process is phosphoric acid on a solid carrier - silicagel. In industrial conditions the process is carried out at a temperature of 180-2200C and pressure (3-4) MPa. The molar ratio of water steam:propylene - (0.4-0.6):1; selectivity of isopropyl alcohol is 95.5% [1, 2]. The service life of the catalyst is 400-500 hours. The activity of the catalyst during operation decreases due of the removal of acid.

In the work [3], it is proposed continuously add H3PO4 to the vapor-gas mixture at the reactor inlet, which ultimately will lead to a large consumption of it. We propose the more expedient method - the method of periodic supply of phosphoric acid due to which the consumption of acid will be significantly reduced. For monitoring the course of the process we

enter the control function 0, equal to the ratio of the current and initial values of phosphoric acid: 0=GWGHCX, actually means the share of its active centers, changing during the operation of the catalyst due to partial acid loss.

Introducing it into the mathematical model of the process proceeding in stationary conditions will keep the productivity of isopro-pyl alcohol at the optimal level for industry and, in addition, will significantly reduce the cost of the process.

Calculation of the process according to the method of periodic feeding

During the starting period of the hydration process (50-100 hours), the maximum removal rate of the acid is observed. However, despite this taking into account the thermody-namic limitations, the amount of acid is still quite large, so the degree of conversion of propylene remains equal to the maximum possible - 4-5)%. During this period the development of the catalyst occurs at which its stable activity is achieved, corresponding to the indicated degree of conversion. The values of 0 in the starting period are close to one. Eventually they decrease. Therefore, in order to preserve the stability of the catalyst, we take 0=0.98 as the criterion value of the control function, when the difference between the current and initial values of phosphoric acid is still small. The accepted

CONTROL OF THE DIRECT HYDRATION PROCESS OF PROPYLENE

16

value of 0 will be adhered throughout the life of the catalyst, assuming that within each 50 hours the removal rate of the acid and the corresponding value of 0 remain almost constant. As experience shows that difference of 0 from the value of 0.98 by approximately 1-2% will already have an effect on the activity of the catalyst and, accordingly, on the output of isopropyl alcohol.

The maximum rate of removal of the phosphoric acid in the starting period for the amount used in the process of 6500 kg is 1.5 kg/h. Then it gradually decreases to (0.05-0.1) kg/h [3].

Calculating the process is presented in Table 1.

At the distribution of the rate of removal of phosphoric acid values over time intervals (50 hours with catalyst life of 500 hours), observed in industry (column 2 of Table 1), the quantities of phosphoric acid Grem which taking out every 50 hours are presented in column 3. The remaining current values of Gcurr and the corresponding values of the control function 0 are presented in columns 4 and 5.

As we can see, in the industrial implementation of the process, when the rate of removal of phosphoric acid is equal to the speed of its continuous supply [3], the adopted value

0=0.98 is violated immediately after the starting period of the catalyst: after 150 hours of operation, 0 decreases to 0.9661 and eventually continues to decrease, i.e. catalyst activity (or the share of its active centers) drops significantly. In this case, taking away, and, therefore, it is brought into the reactor for 500 hours of operation 523.125 kg of phosphoric acid (with its continuous supplying). In order to avoid a large consumption of the catalyst, it is proposed for each time when 0 deviates from the accepted value of 0.98 to add to the remaining amount of phosphoric acid such an additional amount of it, which would lead the catalyst to a stable state.

In this case, the control function will take

G + G G the form: 9' = —^ = -CF-, where the

G G

Ginit Ginit

obtained value G' at this time interval became the initial G' for the following intervals. As we can see from the Table, periodic supplements of phosphoric acid (in the amount of 248.473 kg) instead of continuously supplying it, allow to maintain stable operation of the reactor during the whole period of its operation, and also significantly reduce the consumption of phosphoric acid (248.473 kg instead of 523.125 kg).

Table 1. Comparison of the results of the calculation of the hydration process by industrial and proposed method for its

implementation

Industrial method Proposed method

the time intervals of the catalyst, h rate of removal of phosphoric acid, (by interval) kg/h the amount of phosphoric acid removal in every 50 h, Grem, kg the current amount of phosphoric acid, Gcurr, kg control function 0=Gcun/Gimt (without additives) additives of phosphoric acid, Gadd, kg the current amount of phosphoric acid, kg Gcurr =Gcurr +Gadd control function Q' _ Gcurr + Gadd Ginit (without additives)

0 0 0 6500 1 - - -

0-50 1.5 75 6425 0.9885 - - 0.98

50-100 1.46 73.125 6351.875 0.9772 - - 0.97

100-150 1.42 71.25 6280.625 0.9661 89.375 6370 0.98

150-200 1.35 67.5 6213.125 0.9559 - - 0.98

200-250 1.27 63.75 6149.375 0.946 93.225 6242.6 0.96

250-300 1.05 52.5 6096.875 0.938 - - 0.98

300-350 0.9 45 6051.875 0.9311 65.873 6117.7 0.96

350-400 0.75 37.5 6014.375 0.9253 - - 0.98

400-450 0.6 30 5984.375 0.9206 - - 0.98

450-500 0.15 7.5 5976.875 0.9195 - - 0.98

£523.125 £248.473

By the least squares method [4] using the data of table 1 has been determined the regression dependence to control the hydration process:

y=Gcurr=f(x)=0.0014 • t2- 1.7754 •t+6508.8, (1)

by which it is possible at any time to determine the current value of phosphoric acid (Gcurr) and the corresponding value of 0. Graphically, it is presented in Figure 1.

The dynamics of the change in the control function over time is clearly seen in Figure 2, where the segments below the 0(t) curve mean the quantities of phosphoric acid in the industrial process taking away at the relevant time stage (according Table 1), and the shaded

segments above the curve are those of phosphoric acid we propose to add to the reactor the amount of acid remaining in this time interval in order to comply with the accepted value of 0=0.98, i.e. returning the catalyst to a stable state. As we see in Table 1, they correspond to the addition of phosphoric acid in the amount of 248.473 kg.

The shaded area is the area of stable catalyst activity for 0.98 <0 <1.

Our proposed method of periodic addition of phosphoric acid will significantly reduce the total consumption of acid and maintaining the stability of the catalyst for all 500 hours.

Gcurr

18

CONTROL OF THE DIRECT HYDRATION PROCESS OF PROPYLENE

Mathematical model of the process with taking into account its non-stationarity

The main reaction in the hydrator is the formation of isopropyl alcohol: CH3-CH=CH2+H2O^CH3-CH(OH)-CH3. (2)

The kinetic equation corresponding to this stoichiometric scheme has the form [3]:

^ = kp dt 1

fpо V do

P

■ — x

p0

p

■ — x

Kr P

(3)

where x =

P

IPA

P

Kinetic constants:

k = 9.467 • 109exp

RT

lgKR =

1920 T

— 5.8

(4)

(5)

where KR - equilibrium constant, 1/Pa; \ -rate constant of alcohol formation, 1/(Pa s); P -total pressure of the system, Pa; , Рс°д -

partial pressures of water and propylene at the inlet to the reactor, Pa; P - partial pressure of

isopropyl alcohol, Pa; t - residence time in the reactor, s; x - conversion of propylene.

This model was developed for stationary conditions of the process without taking into account the loss of catalyst activity over time.

Entering the process control function 0 into the kinetic model of the process proceeding under stationary conditions (3), we obtain the non-stationary kinetic model:

dx dt

= kP

f p0 PH,O

Л

P

- — x

PP

\

C3H6

P

- — x

Kr P

e (6)

In deriving the equation of the heat balance were taken into account the heat of the chemical reaction for producing of isopropyl alcohol and the heat going to heat the olefin:

dT

__£ rAH r

Pkat^2 d/ " £ с p)

— Q

heat

(7)

To account for the pressure drop along the length of the reactor was used the Ergun equation [5]:

dP d/

150

"Re

+1.75

PqazM02 (1 — E)

p

• 0.987 -10—55, (8)

where T - reaction temperature, K; pkat - catalyst density, kg/M ; r - rate of reaction, mol/(kgkath); Cpi - heat capacity of the i-th comp onent, kcal/(mol qrad); AHR - heat of reaction, kcal/mol; Qnaq - the heat going to heat the propylene, kcal/mol; ni - the current number of moles of the i-th component, mol/h; Re -

d p m„

pFqaz 0 .

Reynolds criterion equal to

ц (1 — e )

D - diam-

eter of reactor, m; pqaz - gas density, kg/M ; g -acceleration of gravity, M/se; u0 - linear velocity, m/c; dp - equivalent diameter of particles, m; s - porosity, d/q; p, - gas viscosity, kg/(m s); l - length of reactor, m.

The equation of the kinetic model (6) together with the equations of heat balance (7) and pressure loss (8) form the complete mathematical model of the process of direct hydration of propylene taking into account the nonstation-arity of its flowing.

Conclusion

Using this model allow us to maintain the performance of isopropyl alcohol at the desired (stationary) level with the lowest expenditure on the consumption of phosphoric acid.

References

1. Lebedev N.N. Teoriia himicheskikh protcessov osnovnogo organicheskogo i neftehimicheskogo sinteza. M.: Himiia. 1988. 588 s.

2. Zhuravlev V.A. Raschet materialnykh balansov pri proektirovanii proizvodstv organicheskogo sinteza. Uchebnoe posobie. Kemerovo: KuzGTU, 2012. 92 c.

3. Tekhnologicheskif reglament dlia proektirovaniia proizvodstva izopropilovogo spirta moshchnostiu 100 tys. t/god v sostave Sumgaitskogo PO "Sintezkauchuk". 1989 g. 138 s.

4. Balayev V.A., Mammadov N.S. idaraetma obyektlarinin riyazi modeltarinin alinmasi. Baki, 2010. 411 s.

5. Beloglazov I.N., Golubev V.O. Osnovy rascheta filtratcionnykh protcessov. - M.: Izdatelskii dom "Ruda i Metally". 2002. 210 s.

26900

i=1

PROPiLENiN BiRBA§A HiDRATASiYASI PROSESiNiN DiNAMiKASINI NOZORO ALMAQLA

iDARO EDiLMOSi

A.M.Aliyev, A.R.Safarov, I.V.Balayev, A.M.Quseynova, R.Y.Agayeva, F.G.Bayramov

Maqalada propilenin birba§a hidratasiyasi prosesinda fosfor tur§usunun da§iyicidan azalmasi sababindan qeyri-stasionar §araitda izopropil spirtinin mahsuldarliginin a§agi dü§masinin hesablanmasinin aparilmasi göstarilib. Katalizatorun stabil i§inin saxlanilmasi ügün idaraetma funksiyasi taklif olunub. Bu funksiyani prosesin riyazi modelina daxil etmakla izopropil spirtinin mahsuldarligini daimi saviyyada saxlanilmasina imkan veracak.

Agar sözlar: hidratasiya, propilen, izopropil spirti, fosfor tur§usunun slavssi, idar3etm3.

УПРАВЛЕНИЕ ПРОЦЕССОМ ПРЯМОЙ ГИДРАТАЦИИ ПРОПИЛЕНА С УЧЕТОМ ДИНАМИКИ

ЕГО ПРОТЕКАНИЯ

А.М.Алиев, А.Р.Сафаров, И.В.Балаев, А.М.Гусейнова, Р.Ю.Агаева, Ф.Г.Байрамов

Приводится расчет процесса прямой гидратации пропилена, протекающего в нестационарных условиях, вызванных уносом фосфорной кислоты с поверхности носителя и приводящих к снижению производительности установление (реактора) синтеза изопропилового спирта. Для поддержания стабильной работы катализатора предложена функция управления, учет которой в математической модели процесса позволит поддерживать производительность реактора по изопропиловому спирту на постоянном уровне.

Ключевые слова: гидратация, пропилен, изопропиловый спирт, подпитка фосфорной кислотой, управление.