SU1261698A1 - Method of controlling regeneration of saturated absorbent - Google Patents

Abstract

1. METHOD OF MANAGING THE PROCESS OF REGENERATING A SATURATED ABSORBENT, including regulating the pressure of the top of the desorption column by affecting the non-condensable phase after reflux capacity, which is improved by improving the regeneration process and reducing the consumption of water vapor by improving the regeneration process and improving the regeneration process. the columns additionally measure the temperature of the saturated and regenerated solutions of the absorbent at the inlet and outlet of the heat exchanger, as measured by &steam; meters determine the flow rate of water in (A saturated solution of the absorbent and, if the flow rate deviates from the setpoint, adjust the pressure of the top of the desorption column. S o from 00

Description

2. The method according to P.1, about tl u and with the fact that the flow

.Ll s22J I l jL 2 (ti-t,)

e Cf, - 0,52 - I0, 0008 t; (i 1-4)

- heat capacity of dielectric glycol;

- consumption of the regenerated absorbent solution;

- average absorbent concentration in the regenerated solution;

and t,

- temperature of saturated solution

absorbent inlet and outlet heat exchanger, respectively;

and

- the temperature of the regenerated absorbent solution at the inlet and outlet of the heat exchanger, respectively. a solution of absorbent, determined from water in la1661698, is given according to the equation

The invention relates to the automation of the process of integrated gas treatment and to be used in the oil-producing, oil-refining and gas industry.

The aim of the invention is to improve the quality of the regeneration process and reduce the consumption of water vapor by increasing the accuracy of pressure control at the top of the column.

The drawing shows a diagram of the device for implementing the method

The method is carried out as follows.

The saturated absorbent solution (HPA) after absorber 1 through line 2, the passage through heat exchanger 3, is heated by the heat of the regenerated absorbent solution (PPA). The heated HPA, via conduit 4, enters the desorption column 5, where it is divided into two phases. The vapor phase (mainly water vapor and some part of the absorbent) through line 6 leaves on top of the desorption column and, passing through the cooler 7, condenses and enters the reflux tank 8, where the condensate is discharged through line 9, and the non-condensable part is withdrawn through line 10 , the liquid phase in column 5, consisting essentially of.

from the absorbent from the bottom plate of the column, through line 11 goes to the evaporator 12. In the evaporator, it is heated by water vapor fed through line 13. The vapor phase from the top of the evaporator goes through pipe 14 to the blind plate 5 to support temperature of the bottom of the column, and high-temperature PPA from the bottom of the evaporator through the pipeline 15 enters the heat exchanger 3, where, giving some of its heat to the heat exchanger, the HPA,

The conduit 16 is directed to the upper part of the absorber in order to absorb moisture from the gas.

The pressure in the upper part of the column is measured by the sensor 17 and is controlled by the regulator 18 with an impact on the actuator 19, which is set on the withdrawal line of the non-condensable phase.

In the correction chamber of the regulator 18, the signal comes from the computing unit 20, the inputs of which are connected to the sensors 21-25 of the temperature of the HPA and the PPA at the input and output of the heat exchanger 3 and the flow of the PPA, respectively.

The water flow in the HPA is determined in computational unit 20 by equation 2. (t j. ,,, where is Cp, 0.52 + - "- 0.0008 t, (i 1-4) is the heat capacity of the diet langlycol; Z - average concentration of absorbent in PPA; G - consumption of PPA; and t - respectively, HPA temperature at the inlet and outlet of the heat exchanger; t, j and t, - respectively, the FPA temperature at the inlet and outlet of the heat exchanger .In each case, depending on the depth of drying gas, the value of Z is set and entered into the computing unit, manually. For the northern regions, 993 is assumed. The increase in water consumption in the NRA leads to an increase in of the vapor phase and the increase in pressure in the upper part of the Hbi desorption column, since the HPA temperature at the inlet of the Bbmie column (100-120 ° C), the more water in the HPA, the t4.C.4) (J -ZKt4., ). its evaporation and the amount of separated water vapor in the column will be greater, and this is equivalent to an increase in the pressure of the top of the column. Consequently, with increasing water flow in the HPA, the pressure at the top of the desorption column will increase. Therefore, to ensure a predetermined pressure at the top of the column with increasing water flow in the HPA against the inlet, it is necessary to increase the flow of the non-condensable phase and vice versa. If other parameters are constant, the lower the HPA temperature at the exit of the heat exchanger according to equation (1), the greater the flow rate of water in the HPA. Consequently, the pressure of the top of the column will be greater than the nominal one and at the same time, in order to achieve a given pressure value, it is necessary to increase the flow rate of the noncondensable phase being withdrawn after the reflux tank affecting the actuator 19, which ensures the pressure invariance to the perturbation from the water flow in the HPA, and thus increases pressure control.

Claims (2)

1. METHOD FOR CONTROLLING THE PROCESS OF REGENERATION OF A SATURATED ABSORBENT, including regulating the pressure of the top of the desorption column by affecting the removal of the non-condensable phase after the reflux capacity, characterized in that, in order to improve the quality of the regeneration process and reduce the flow of water vapor by improving the accuracy of regulation of the pressure of the column top additionally measure the temperature of the saturated and regenerated absorbent solutions at the inlet and outlet of the heat exchanger, the measured flow rate is determined Water in a saturated solution of absorbent and when the water flow deviates from the set value, the top pressure of the desorption column is adjusted. go 2. The method according to claim 1, differing saturation solution absorbent opredesch and I th with the fact that the water flow in la-- lyayut by the equation "h £ (1 ^{_ Z) (t ^ -ti)} _, ⁶ ~ t _a “T. where C ‘ = 0.52 + absorbent on + 0,0008 t; (i = entrance and exit - = 1-4) - heat capacity de heat transfer - e tipengen glycol; nickname G - flow rate nno; bath solution t, and C - temperature absorbent; generated - Z - average concentration th solution absorbance absorbent on regenerated inlet and outlet a solution; heat exchanger H and t _a - temperature accordingly - solution but.