RU2692719C1 - Method for cleaning process condensates using an intermediate container - Google Patents

Abstract

FIELD: technological processes.SUBSTANCE: invention can be used in chemical industry. Process condensates removal from hydrogen sulphide and ammonia is carried out in two series-connected columns equipped with mass exchange devices: a column for extracting hydrogen sulphide 1 and a column for producing purified waste water 2, removing purified waste water 13 from said system, gaseous hydrogen sulphide 18 and ammonia gas mixture with residual hydrogen sulphide and water 20. Purified waste water 21 is withdrawn from column 2 and cooled down with formation of purified waste water 13, part of cooled purified waste water 31 is returned to the upper part of hydrogen sulphide extraction column 1. Gas mixture of ammonia with residual hydrogen sulphide and water 28 is supplied for further purification into ammonia purification absorber 3 with ammonia discharge lines 22 from above and saturated absorbent 26 from below. Gaseous mixture of ammonia with residual hydrogen sulphide and water 20 is cooled in condenser 10 and fed into intermediate tank 12, the liquid phase from which is removed as recycle stream 27 into the hydrogen sulphide extraction column 1, and gas mixture 28 – into absorber 3 under nozzle layer 14. Absorbent 23 is obtained by mixing ammonia vapours 22 with treated waste water 30. Absorbent 23 after mixing is cooled in heat exchanger 11, supplied into absorbent container 4, then supplied to layer of absorber 3 nozzle 14. Gaseous ammonia 24 and / or ammonia water 25 is removed from absorbent container 4. Flow of saturated absorbent 26 is discharged from absorber 3 to upper part of column 2.EFFECT: invention provides higher degree of purification of process condensates and waste components.4 cl, 1 dwg, 1 tbl

Description

The invention relates to the refining, petrochemical industry and is intended for the deep cleaning of process steam condensates (also called wastewater) from hydrogen sulfide and ammonia, including the purification of sulfide-containing alkaline waste water, to produce ammonia, hydrogen sulfide, and possibly ammonia water with a high degree purity.

The known method of purification of process condensates (see Karelin YA.A. and others. Wastewater treatment of refineries. M: Stroyizdat, 1982, p. 51-53) by two-step separation using the methods of stripping and distillation with obtaining at the first stage of separation Stripping column of hydrogen sulfide as the head product and water enriched in ammonia with a residual content of hydrogen sulfide as a residue, with the concentration of hydrogen sulfide at the top of the absorption and stripping column through the interaction of water vapor enriched in se hydrogen, with cooled and purified waste water on the plates, with the supply of purified waste water from the bottom of the absorption and stripping column to the distillation column with sharp irrigation in the second separation stage to produce a vapor-gas mixture of water and ammonia with a residual hydrogen sulfide content as the head product and purified condensate water as a residue, followed by condensation of a vapor-gas mixture of water and ammonia with residual hydrogen sulfide in a condenser-cooler, separating the resulting vapor-gas mixture si in the separator and the recirculation of the liquid phase in the absorption-stripping column on the first stage of separation.

The disadvantage of this method is the low degree of purification of process condensate (water), low quality hydrogen sulfide and ammonia-containing gases and, due to this, the formation of crystalline salts of sulfide and ammonium hydrosulfide on the dry cold surfaces of the hardware components: the bottom surfaces and in the overflow devices of the plates or on the nozzles and collectors and distributors of liquid packed columns, in the condensation units and separation of gas mixtures of columns and pipelines of product gas flows, which leads to neo go steaming or rinsing installation data elements, which increases the operating costs of the process.

A known method of purification of process condensates, in which the additional purification of the stream is carried out in the scrubber packing layer by absorbing ammonia by the cooled liquid flow, heat in the distillation column is removed by circulation irrigation, and ammonia is cleared from hydrogen sulfide residues in a packing scrubber with circulation irrigation (see RU 2162444, publ. January 27, 2001, IPC C02F 1/04).

The closest analogue chosen for the prototype of the invention is a method of purification of process condensates from hydrogen sulfide and ammonia, including the supply of untreated process condensates as a power supply for a system of columns equipped with mass transfer devices, the system of columns is carried out in the form of two successively connected columns: columns of hydrogen sulfide separation and receiving columns purified waste water, with the removal of purified waste water, hydrogen sulfide gas, and ammonia gas with residual gas from this system m hydrogen sulfide and water, cooling in the heat exchanger of treated wastewater discharged from the column to form cooled purified wastewater withdrawn from the specified system, returning part of the cooled purified wastewater to the top of the hydrogen sulfide release column, feeding the ammonia gas with residual hydrogen sulfide and water for additional purification ammonia purification absorber with ammonia removal lines on top of the ammonia purification absorber and saturated ammonia purification absorber from the bottom, aftertreatment of ammonia gas mixture with wasps the hydrogen sulfide and water is carried out in an absorber for cleaning ammonia with an absorbent, see EN 2307795 C1, publ. 10.10.2007, IPC C02F 1/04. For the purification of ammonia in the prototype, a two-stage absorber is used, in the first stage the flow of ammonia is washed with purified waste water, and in the second stage it is cooled with circulation irrigation.

Using the installation of an additional absorber and purification of ammonia-containing gas in two stages, it was possible to reduce the concentration of hydrogen sulfide in it, as well as reduce the likelihood and rate of formation in cold streams of crystalline sulfides and ammonium hydrosulfides, however, a sufficiently high residual content of hydrogen sulfide in the ammonia stream (0.01 wt. %), sometimes still leads to clogging of the equipment and pipelines, and the resulting ammonia requires further purification of the ammonia gas from hydrogen sulfide before it is used generation or disposal. Therefore, the disadvantage of the prototype method is the high content of impurities in the product flow of the installation, primarily the high content of hydrogen sulfide in the stream of ammonia, and high energy costs for carrying out the process of separation of products.

The problem to which the invention is directed is to increase the degree of purification of process condensates, reduce the content of hydrogen sulfide in the stream of ammonia and ammonia in the stream of hydrogen sulfide, reduce the likelihood of formation of ammonium hydrosulfide salts in apparatus and pipelines, and ensure the continuous operation of the purification plant for technological condensates.

The technical result of the invention is to increase the degree of purification of process condensates and waste components, reducing the operating costs of the process.

According to the invention, the method of purification of process condensates from hydrogen sulfide and ammonia includes: supplying crude process condensates as a power supply to a system of columns equipped with mass transfer devices, the system of columns is carried out in the form of two columns connected in series: columns of hydrogen sulfide separation and a column for obtaining purified process condensate (hereinafter - purified waste) water), with the conclusion from this system of purified waste water, gaseous hydrogen sulfide and ammonia gas mixture with residual hydrogen and water, cooling in the heat exchanger of treated wastewater discharged from the column to form cooled purified wastewater discharged from the specified system, returning part of the cooled purified wastewater to the upper part of the hydrogen sulfide release column, supplying the ammonia gas with residual hydrogen sulfide and water for additional purification to the absorber purification of ammonia with ammonia removal lines on top of the absorber for purifying ammonia and a saturated absorbent at the bottom of the absorber for purifying ammonia, after-treatment of the ammonia gas mixture with residual Full-time hydrogen sulfide and water is carried out in an absorber for cleaning ammonia with an absorbent.

New is that the gas mixture of ammonia with residual hydrogen sulfide and water is cooled in the vapor condenser of the column for obtaining purified waste water and then fed into an intermediate tank, the liquid phase from which the bottom of the tank is discharged as a recycle stream into the column of hydrogen sulfide evolution below the crude process condensates, and the gas mixture - in the ammonia purification absorber under the nozzle layer, the absorbent is obtained by mixing ammonia vapor leaving the ammonia purification absorber with purified waste water from the purified wastewater stream from the column for obtaining purified wastewater, the absorbent after mixing is cooled in the heat exchanger, and after cooling it is fed into the absorbent tank, then the cooled absorbent is fed from the absorbent tank to the ammonia purification nozzle layer of the absorber, removing ammonia gas and / or ammonia water from the capacity of the absorbent, while the flow of the saturated absorbent is removed from the absorber purification of ammonia on the upper part of the column to obtain purified waste water.

In the inventive method, crude process condensates can be supplied to the hydrogen sulfide recovery column in two streams: cold stream and hot stream heated in the heat exchanger of heating the raw material.

In the method according to the invention, the successive connection of a hydrogen sulfide recovery column and a column for obtaining purified waste water can be carried out along the line of removal of hydrogen sulfide from the hydrogen sulfide from the bottom of the column and cooled in a refrigerator and injected into the top of the column to obtain purified waste water. Such a series connection of a hydrogen sulphide separation column and a column for the production of purified waste water may include an additional connection of a drain line from the bottom of the column for the discharge of hydrogen sulfide from waste water with a column for obtaining purified waste water before cooling in a refrigerator below the connection of the line after cooling in a refrigerator, with a column for obtaining purified waste water .

The invention is illustrated by figure 1, which shows a schematic flow diagram of the purification of process condensates from hydrogen sulfide and ammonia according to the proposed method.

The positions on the proposed figure denote: 1 - a column of hydrogen sulfide; 2 - column for obtaining purified waste water; 3 - ammonia purification absorber; 4 - absorbent capacity; 5 - reboiler of hydrogen sulfide recovery column; 6 - reboiler of the column receiving purified waste water; 7 - heat exchanger for heating raw materials; 8 - refrigerator raw materials columns for obtaining purified waste water; 9 - refrigerator of purified waste water; 10 - vapor condenser of the column receiving purified waste water; 11 - refrigerator cooling absorber; 12 - intermediate capacitance of the vapor condenser of the column to obtain purified waste water; 13 - line withdrawal from the system of treated wastewater; 14 - nozzle absorber 3; 15 - supply line untreated process condensates in column 1; 16 - supply line cold unheated stream of crude process condensates in column 1; 17 - supply line of the heated stream of crude process condensates in column 1; 18 - line withdrawal from the system of pure gaseous hydrogen sulfide; 19 - line withdrawal from the bottom of the column 1 of process condensates, purified from hydrogen sulfide; 20 - line output of the gas mixture of ammonia with residual hydrogen sulfide and water; 21 - line output purified wastewater from column 2; 22 - line of ammonia removal from the top of the absorber 3; 23 - line output from the container 4 of the absorbent and feed it into the absorber 3; 24 - line output from the system of pure gaseous ammonia; 25 - line output from the system of pure ammonia water; 26 - line output from the absorber 3 of the saturated absorbent in the column 2; 27 is a supply line for the liquid phase from the intermediate tank to the column 1; 28 - gas supply line from the intermediate tank to the absorber 3; 30 - supply line of treated wastewater from line 13 for mixing with ammonia vapors through line 22, with the mixture fed to the cooling heat exchanger 11; 31 - supply line of treated wastewater from line 13 to column 1; 32 - the line from the refrigerator 8 to the top of the column 2. The listed lines can be pipelines.

The method of purification of process condensates from hydrogen sulfide and ammonia is carried out by a purification system operating according to the rectification method as follows.

Line 15 serves crude process condensates as feed for a column system equipped with mass transfer devices. The system of columns is carried out in the form of two columns connected in series: columns 1 of hydrogen sulfide separation (absorption and stripping columns) and column 2 for obtaining purified waste water (distillation column), with output of purified technological condensates through line 13 from this system, hydrogen sulfide gas through line 18 and line 20 - gas mixture of ammonia with residual hydrogen sulfide and water. Sequential connection of the column 1 of hydrogen sulfide and the column 2 to obtain purified wastewater can be carried out through the line 19 from the bottom of the column 1, the separation of hydrogen sulfide from waste water, purified from the main amount of hydrogen sulfide, with its cooling in the refrigerator 8 and entering through line 32 into the upper part of the column 2 receiving purified waste water (below the outlet of the gas mixture through line 20). Such a series connection of the hydrogen sulphide separation column 1 and the column 2 for obtaining purified wastewater may include an additional connection of line 19 with column 2 before cooling in refrigerator 8 below connection of line 32, after cooling in refrigerator 8, to reduce operating costs.

From the bottom of the column 2 for receiving purified waste water, the treated waste water is discharged through line 21 for cooling to the heat exchanger 9 with the formation of cooled purified waste water discharged from the specified system through line 13. A part of purified waste water formed in line 13 is returned via additional line 31 in the upper part of the column 1 release of hydrogen sulfide (below the outlet of gaseous hydrogen sulfide in line 18).

On line 20, the ammonia gas mixture with residual hydrogen sulfide and water is cooled in the condenser 10 of the vapor column 2 to obtain purified waste water, and then fed into the intermediate tank 12 to purify the ammonia gas mixture from hydrogen sulfide residues. Intermediate tank 12 may be, for example, a vessel in the form of a gravity separator with inlets and outlets, as shown in Figure 1. The liquid phase with hydrogen sulfide residues from the bottom of tank 12 is discharged through line 27 as a recycle stream into the column 1 of hydrogen sulfide release below the raw supply line 15 technological condensates. The purified gas mixture from the upper part of the intermediate tank 12 is discharged through line 28 to the ammonia purification absorber 3 under the nozzle layer 14 (to the lower part of the absorber 3, under the nozzle 14, but higher than the outlet through the saturated absorbent flow line 26).

The ammonia purification absorber 3 has an ammonia removal line 22 at the top of the ammonia purification absorber 3, a saturated absorbent removal line 26 at the bottom of the ammonia purification absorber 3 into the column 2.

Subsequent purification of the gas mixture of ammonia supplied through line 28, is carried out in the absorber 3 purification of ammonia by the absorbent. The specified absorbent is obtained by mixing ammonia vapors leaving through line 22 from the absorber 3 for purifying ammonia with purified wastewater supplied through line 30 from the stream of purified wastewater formed in line 13 from the column 2 for producing purified wastewater.

The specified absorbent after the specified mixing is cooled in the heat exchanger 11, where there is a partial dissolution of ammonia in a stream of water with the formation of a cold stream of absorbent (ammonia water), and after cooling, served on line 18 in the container 4 of the absorbent. In the tank 4, the vapor-liquid stream is separated into gaseous ammonia and a liquid absorbent (ammonia water). The container 4 may be, for example, a vessel in the form of a gravity separator with inlets and outlets, as shown in FIG. 1.

After the absorbent tank 4, the cooled absorbent is fed through line 23 from tank 4 to nozzle layer 14 (to the upper part of the absorber, above nozzle 14) of the ammonia purification absorber 3 (but below the ammonia vapor removal through line 22). Ammonia gas is discharged through line 24 on top of the absorbent container 4, while pure ammonia water can be removed from the bottom of the absorber container 4 from the system 25. Only ammonia gas, or only ammonia water, or both can be withdrawn.

Untreated sewage (process condensates) through line 15 can be fed into the top of the hydrogen sulfide separation column 1 (below the hydrogen sulfide gas outlet through line 18) in two streams: unheated (cold) stream through line 16 and heated (hot) stream through line 17. Hot the stream is heated in the heat exchanger 7 for heating the raw material.

The flow of saturated absorbent is removed from the bottom of the absorber 3 purification of ammonia through line 26 to return to the upper part of the column 2 to obtain purified waste water (below the outlet of the gas mixture through line 20).

The inventive cleaning method is as follows.

Food in the form of crude process condensates through line 15 is fed to the hydrogen sulfide separation column 1 by the streams described above. In the bottom of the column 1, the release of hydrogen sulfide using reboiler (heat exchanger) 5 is supplied heat. In column 1, hydrogen sulfide is stripped from sulphide-containing effluent. At the top of the column 1, the hydrogen sulfide stream is purified from ammonia residues with purified waste water coming in line 31.

The sulfide-containing effluent purified from hydrogen sulfide through line 19 is discharged from the bottom of the column 1, cooled in the refrigerator 8 and fed to the column 2 to obtain purified waste water. Into column 2, a stream of saturated absorbent is also supplied via line 26 from absorber 3. Heat is supplied to the bottom of column 2 using a reboiler (heat exchanger) 6. In column 2, ammonia and hydrogen sulfide residues are stripped off. From the bottom of the column 2 through line 21 is discharged purified water cooled in the heat exchanger 9.

Ammonia vapors with water and hydrogen sulfide residues through line 20 are removed from column 2 for obtaining purified waste water, condensed in the vapor condenser of the column for obtaining purified waste water 10 and are fed into intermediate tank 12. In intermediate tank 12, the ammonia stream is purified from residual hydrogen sulfide. The liquid phase with hydrogen sulfide residues from the bottom of the tank 12 is discharged via line 27 as a recycle stream to the hydrogen sulfide separation column 1 below the crude process condensate supply line 15. The purified gas mixture from the top of the intermediate tank 12 is discharged via line 28 to the ammonia purification absorber 3. Pure ammonia is removed from the absorber through line 22, mixed with purified wastewater supplied through line 30, cooled in the refrigerator 11 and fed into the absorbent container 4.

Pure ammonia gas through line 24 and / or pure ammonia water through line 25 can be removed from the absorbent tank 4 via line 25. Options are possible with a joint output along lines 24 and 25, respectively, of pure ammonia and pure ammonia, and with only pure ammonia through 24, or with the conclusion only pure ammonia water through line 25. Through line 23, absorber 3 is supplied to absorber 3. Saturated absorbent from the absorber 3 is displayed on line 26 to the top of column 2.

Due to the presence of an intermediate tank 12 for cleaning the ammonia gas mixture from hydrogen sulfide residues, ammonia is pre-cleaned from hydrogen sulfide, while hydrogen sulfide residues through line 27 return to the initial purification stage (in column 1), which ultimately leads to an increase in the degree of purification of process condensates and waste components, as well as to reduce the operating costs of the process.

Due to the fact that the absorbent used for the purification of ammonia is obtained by dissolving ammonia in purified waste water while simultaneously cooling the stream, this avoids heating the absorbent during dissolution, to obtain a cold saturated solution of ammonia water and thereby more efficiently purge the ammonia stream from hydrogen sulfide . Otherwise, the heating of the absorbent when fed to the absorber of the absorbent obtained by dissolving ammonia in water, followed by cooling, and even more so when pure water or purified waste water is supplied to the absorber, leads to an increase in the temperature of the absorbent, which leads to a decrease in the efficiency of absorption of hydrogen sulfide from the ammonia stream, as it happened in the prototype.

Due to the effective absorption of hydrogen sulfide from the ammonia stream, the consumption of absorbent is reduced, which also leads to a decrease in the absorbent recycle stream and a decrease in the concentration of ammonia in the column system. All this leads to a reduction in the energy costs of separation and improves the degree of purification of wastewater and waste products.

Due to the fact that the ammonia gas mixture with residual hydrogen sulfide and water, going through line 20, is cooled in condenser 10, this mixture is supplied with a lower temperature, which has a positive effect on the further purification of this gas mixture and the degree of purification of process condensates and waste components whole

Due to the fact that the flow of saturated absorbent through line 26 is removed from the absorber 3 purification of ammonia to the upper part of the column 2 to obtain purified waste water, and the liquid stream with hydrogen sulfide residues through line 27 from the intermediate tank 12 as a recycle stream into the column 1 release of hydrogen sulfide below the input untreated process condensates 15, it allows to reduce the concentration of ammonia on the upper plates of the column and to reduce the consumption of treated wastewater for the purification of hydrogen sulfide from ammonia. The flow through line 26 to the top of the column 2 of wastewater treatment reduces the temperature of the top of the column 2 to obtain purified wastewater and the load on the condenser 10 of the vapor column to obtain purified wastewater, which ultimately improves the degree of purification of wastewater and waste components.

Due to the fact that the liquid stream with hydrogen sulfide residues from the intermediate tank 12 is returned via line 27 as a recycle stream to the hydrogen sulfide separation column 1 below the feed stream of the column, i.e. below the input of the untreated process condensates 15 and regardless of it, this will allow better and better separation of hydrogen sulfide from the wastewater without mixing these streams at the entrance to the column 1 of hydrogen sulfide emissions. With joint feed, i.e. when feeding a liquid stream through line 27 to the feed inlet of the column, i.e. The quality of the hydrogen sulfide stream deteriorates into the untreated sewage stream 15, as it was in the prototype, before entering the hydrogen sulfide recovery column.

The use of the described scheme with columns 1, 2, intermediate tank 12, absorber 3 and capacity 4 reduces the energy costs of separation and ensures stable operation of the column system even when emulsions come in for cleaning as part of crude process condensates, recycled ammonia condensates from individual sources.

The cleaning of process condensates occurs with the following parameters of the process mode:

1. Pressure, kg / cm ² (excess):

Column 1 2.0 - 8.0 Column 2 0.2-3.0 Absorber 3 0.2-3.0

2. Temperature, top of apparatuses ° С:

Column 1 35-60 Column 2 35-125 Absorber 3 35-45

Achieved degree of purification of process condensates:

from hydrogen sulfide:

- before cleaning 4000-50000 mg / kg,

- after cleaning not more than 1 mg / kg;

from ammonia

- before cleaning 4000-50000 mg / kg,

- after cleaning not more than 5 mg / kg.

As gas products receive:

hydrogen sulfide with an ammonia content of not more than 1 mg / kg,

ammonia with a hydrogen sulfide content of not more than 1 mg / kg.

Simultaneously with or instead of gas ammonia, a saturated aqueous solution of ammonia with a hydrogen sulfide content of not more than 1 mg / kg can be obtained.

As an example, an installation for cleaning process condensates with a capacity of 55 m ³ / h is given.

The absence of hydrogen sulfide in the flow of ammonia and ammonia in the flow of hydrogen sulfide (not more than 1 mg / kg in the claimed method versus not more than 0.01 wt.% In the prototype, which corresponds to 100 mg / kg) will avoid blockage of the equipment and pipelines, which will significantly reduce operational, energy costs for the process of separation of products.

An example of the parameters of the main apparatus of the system are presented in Table. one.

This method allows to obtain purified waste water with a hydrogen sulfide content of not more than 1 mg / kg (in the example 1 mg / kg) and ammonia no more than 5 mg / kg (in the example 4 mg / kg), hydrogen sulfide with an ammonia content not more than 1 mg / kg (in the example - 1 mg / kg), ammonia and / or ammonia water with a hydrogen sulfide content not exceeding 1 mg / kg (in the example, 0 and 1 mg / kg, respectively) when cleaning process condensates.

Thus, the application of the proposed method allows to increase the degree of purification of process condensates and product streams, with the possibility of selecting a pure aqueous solution of ammonia, as well as to reduce the operating costs of the process and emissions of harmful pollutants into the environment. Additionally, the possibility of selecting a pure aqueous solution of ammonia.

Claims (15)

1. The method of cleaning process condensates from hydrogen sulfide and ammonia, including: supply of crude process condensates (15) as a power supply for a system of columns equipped with mass transfer devices, the system of columns is carried out in the form of two columns connected in series: columns (1) of separating hydrogen sulfide and a column (2) of obtaining purified waste water, with output from this system of purified waste water (13), gaseous hydrogen sulfide (18) and a gas mixture (20) of ammonia with residual hydrogen sulfide and water, cooling in the heat exchanger (9) of the treated wastewater (21) discharged from the column (2) with the formation of cooled purified wastewater (13) discharged from the specified system, returning part of the cooled purified waste water (31) to the top of the column (1) of hydrogen sulfide recovery, supplying the ammonia gas mixture (20) with residual hydrogen sulfide and water for additional purification to the ammonia purification absorber (3) with ammonia drain lines (22) on top of the ammonia purification absorber (3) and ammonia and absorber saturation (26) from the bottom of the ammonia purification absorber (3), aftertreatment of the gas mixture (20) of ammonia with residual hydrogen sulfide and water is carried out in the absorber (3) the purification of ammonia with an absorbent, characterized in that ammonia gas mixture (20) with residual hydrogen sulfide and water is cooled in the condenser (10) of the column vapor (2) to obtain purified waste water and then fed to the intermediate tank (12), the liquid phase from which the bottom of the tank (12) is discharged as a recycle stream in the column (1) hydrogen sulfide emission is lower than the input of crude process condensates (15), and the gas mixture (28) - into the absorber (3) of ammonia purification under the nozzle layer (14), said absorbent is obtained by mixing ammonia vapors (22) leaving the absorber (3) for purifying ammonia, with purified waste water (30) from the stream of purified waste water (13) from the column (2) for obtaining purified waste water, After mixing, the absorbent is cooled in a heat exchanger (11), and after cooling it is fed into the container (4) of the absorbent, then the cooled absorbent is fed from the container (4) of the absorbent to the layer of nozzle (14) of the absorber (3) for ammonia purification, removing the gaseous ammonia (24 ) and / or ammonia water (25) from the container (4) of the absorbent, the stream of saturated absorbent (26) is removed from the absorber (3) of ammonia purification to the upper part of the column (2) to obtain purified waste water. 2. The method of purification of process condensates from hydrogen sulphide and ammonia under item 1, characterized in that the crude process condensates (15) are fed into the column (1) of the separation of hydrogen sulphide by two streams: cold stream (16) and hot stream (17) heated in heat exchanger (7) heating the raw material. 3. The method of purification of process condensates from hydrogen sulfide and ammonia under item 1, characterized in that the serial connection of the column (1) of the separation of hydrogen sulfide and the column (2) of obtaining purified waste water is carried out along the line (19) from the bottom of the column (1) of the separation of hydrogen sulfide waste water, purified from hydrogen sulfide, with its cooling in the refrigerator (8) and entering into the upper part of the column (2) to obtain purified waste water. 4. The method of purification of wastewater from hydrogen sulfide and ammonia under item 3, characterized in that the series connection of the column (1) of the separation of hydrogen sulfide and the column (2) of obtaining purified waste water includes an additional connection of the line (19) of the bottom of the column (1) of the allocation hydrogen sulfide waste water with a column (2) before cooling in the refrigerator (8) below the connection line (32), going after cooling in the refrigerator (8), with the column (2) to obtain purified waste water.

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