A coking wastewater ammonia distillation treatment device relates to the field of chemical production, and aims to solve the problems that the conventional ammonia distillation stripping tower generally adopts a full-stripping process route, the ammonia distillation process has the defects of low concentration of prepared ammonia water, high H2S content and standard exceeding of liquid ammonia content in a tower kettle, the device comprises a stripping tower, a reboiler, a feed cooler, an acid separator, a purified water pump and a fractional condensation liquid cooler, the top end of the stripping tower is connected with the acid separator, the one-level dephlegmator is connected through the one-level preheater at the stripper middle part, stripper bottom one end is connected to the second grade preheater through purified water pump, and the other end passes through the reboiler and connects back stripper bottom, the utility model discloses, thoroughly solve traditional technology aqueous ammonia concentration low, H2S high content, tower cauldron liquid ammonia content scheduling problem that exceeds standard, increase the environmental protection problem that the loss of second grade cold feed system has avoided the ammonia resource is extravagant and has caused.
Description Coking wastewater ammonia distillation treatment deviceTechnical Field
The utility model belongs to the chemical production field, concretely relates to coking wastewater ammonia distillation treatment device.
Background
In recent years, the environmental problem that the residual ammonia water in the coke-oven plant carries rice is increasingly serious. The coking industry discharges about thousands of tons of ammonia-containing wastewater every year, so that a plurality of rivers and lakes are polluted. Because the coking wastewater treatment technology is at a lower level when the coking is designed and constructed at that time, the treatment of the ammonia-containing wastewater is under development, most of the domestic common biochemical technologies of factories have little effect on the degradation of ammonia nitrogen pollution, and the ammonia nitrogen in the discharged water is seriously out of standard. The discharge of the waste water causes great pollution to the received water body, so that the water body generates eutrophication and the use function of the water body is influenced.
The common biochemical treatment widely used in coking plants basically comprises facilities and equipment such as an oil removal tank, a regulating tank, a flotation tank, an aeration tank, a sludge sedimentation tank, a coagulating sedimentation tank, a blower and the like, and because the ammonia concentration is too high, the wastewater is mixed and sent to an ammonia still to remove most ammonia nitrogen pollutants before entering the biochemical treatment. The traditional ammonia distillation stripping tower generally adopts a full-stripping process route, and the ammonia distillation process has the problems of low concentration of prepared ammonia water, high H2S content, overproof liquid ammonia content in a tower kettle and the like.
SUMMERY OF THE UTILITY MODEL
The ammonia distillation process aims to solve the problems that the concentration of prepared ammonia water is low, the H2S content is high, and the liquid ammonia content in a tower kettle exceeds the standard.
The utility model discloses a coking wastewater ammonia distillation treatment device, which comprises a raw material water tank, a raw material water pump, a stripping tower, a reboiler, a feeding cooler, an acid separator, a purifying water pump, a secondary preheater, a primary dephlegmator, a secondary condenser, a secondary dephlegmator, a tertiary condenser, a tertiary dephlegmator and a dephlegmator cooler;
the bottom of the raw material water tank is divided into two paths by a raw material water pump, one path is connected with the middle upper part of the stripping tower through a feeding cooler, and the other path is connected to the middle part of the stripping tower through a primary preheater and a secondary preheater in sequence;
the top end of the stripping tower is connected with an acid separator, the middle part of the stripping tower is connected with a primary dephlegmator through a primary preheater, one end of the bottom of the stripping tower is connected to a secondary preheater through a purification water pump, and the other end of the bottom of the stripping tower is connected to the bottom of the stripping tower through a reboiler;
the bottom end of the acidic separator is connected with the middle part of the raw material water tank;
the top of the first-stage dephlegmator is connected with the middle part of the second-stage dephlegmator through a second-stage condenser, and the top of the second-stage dephlegmator is connected with a third-stage dephlegmator through a third-stage condenser;
the bottom of the first-stage partial condenser and the bottom of the second-stage partial condenser are communicated with the bottom of the third-stage partial condenser through a condensate cooler and then are connected to the middle part of the raw material water tank.
The low-pressure steam passes through an acid separator to remove steam condensate.
The utility model discloses the advantage:
use the utility model discloses, adopt single tower strip, the technology of side draw out, thoroughly solve traditional technology aqueous ammonia concentration low, H2S content high, tower cauldron liquid ammonia content scheduling problem that exceeds standard, increase the environmental protection problem that the loss of second grade cold feed system avoided the ammonia resource is extravagant and cause, increase the side stripping tower, the strip tower middle part sets up a plurality of gas phase outlets, according to material component or the technological requirement of difference, can select different ammonia vapor side draws the export that contains.
Drawings
Fig. 1 is a schematic view of the present invention;
description of the reference numerals:
1. a raw material water tank; 2. a raw material water pump; 3. a stripping column; 4. a reboiler; 5. a feed cooler; 6. acid gas partial condenser; 7. purifying the water pump; 8. a secondary preheater; 9. a primary preheater; 10. a first-stage dephlegmator; 11. a secondary condenser; 12. a secondary dephlegmator; 13. a third-stage condenser; 14. a third-stage dephlegmator; 15. a condensate separating cooler.
Detailed Description
As shown in fig. 1:
a coking wastewater ammonia distillation treatment device comprises a raw material water tank 1, a raw material water pump 2, a stripping tower 3, a reboiler 4, a feeding cooler 5, an acid separator 6, a purification water pump 7, a secondary preheater 8, a primary preheater 9, a primary dephlegmator 10, a secondary condenser 11, a secondary dephlegmator 12, a tertiary condenser 13, a tertiary dephlegmator 14 and a dephlegmator cooler 15;
the bottom of the raw material water tank 1 is divided into two paths through a raw material water pump 2, one path is connected with the middle upper part of the stripping tower 3 through a feeding cooler 5, and the other path is connected with the middle part of the stripping tower 3 through a primary preheater 9 and a secondary preheater 8 in sequence;
the top end of the stripping tower 3 is connected with an acid separator 6, the middle part of the stripping tower 3 is connected with a primary dephlegmator 10 through a primary preheater 9, one end of the bottom of the stripping tower 3 is connected with a secondary preheater 8 through a purified water pump 7, and the other end of the bottom of the stripping tower 3 is connected back to the bottom of the stripping tower 3 through a reboiler 4;
the bottom end of the acid separator 6 is connected with the middle part of the raw material water tank 1;
the top of the first- stage dephlegmator 10 is connected with the middle of a second- stage dephlegmator 12 through a second- stage condenser 11, and the top of the second- stage dephlegmator 12 is connected with a third- stage dephlegmator 14 through a third- stage condenser 13;
the bottom of the first-stage partial condenser 10 and the bottom of the second-stage partial condenser 12 pass through a condensate cooler 15 and then are communicated with the bottom of the third-stage partial condenser 14 to be connected to the middle part of the raw material water tank 1.
The low pressure steam passes through the sour separator 6 to remove steam condensate.
The working process comprises the following steps: the residual ammonia water from the coking process enters a raw material water tank 1 after being pretreated, the residual ammonia water is pressurized by a raw material water pump 2 and then is divided into two paths, one path of the residual ammonia water is used as cold feeding and enters the upper part of a stripping tower 3 after being cooled by a feeding cooler 5, the other path of the residual ammonia water is used as hot feeding and firstly carries out primary heat exchange with side gas through a primary preheater 9, and then carries out secondary heat exchange with tower bottom liquid through a secondary preheater 8, and then the residual ammonia water enters the middle upper part of the stripping tower 3 for stripping, the stripping tower 3 utilizes low-pressure steam as a heat source, and the tower bottom circulating liquid is heated by a reboiler 4 and then returns to the stripping tower 3.
Free ammonia, carbon dioxide, hydrogen sulfide and other non-condensable gases are continuously transferred from the liquid phase to steam, and when the free ammonia, the carbon dioxide, the hydrogen sulfide and other non-condensable gases reach the upper section of the stripping tower 3, most of the free ammonia, the carbon dioxide, the hydrogen sulfide and other non-condensable gases enter a gas phase; cold feed flowing from top to bottom absorbs ammonia and water vapor in the gas phase, when the cold feed is discharged from the top of the stripping tower 3, the main components of the acid gas are carbon dioxide and hydrogen sulfide, the content of ammonia reaches a designed value, the ammonia gas is discharged from the stripping tower 3, the ammonia gas enters the acid gas separator 6 for gas-liquid separation, the separated liquid phase returns to the raw material water tank, and the acid gas is discharged out of the device after being heated by low-pressure steam.
In an ammonia enrichment area in the middle of the stripping tower 3, ammonia-containing steam is extracted from the lateral line of the stripping tower 3, the ammonia-containing steam extracted from the lateral line is cooled step by a first- stage condenser 9, a second- stage condenser 11 and a third- stage condenser 13, then is subjected to gas-liquid separation in a first- stage dephlegmator 10, a second- stage dephlegmator 12 and a third- stage dephlegmator 14, a liquid phase separated in the first stage and the second stage is cooled by a dephlegmator cooler 15, then is mixed with a liquid phase separated in the third stage, and then returns to the raw material water tank 1 again, and a pure ammonia gas separated from the third- stage dephlegmator 13 is led out of the device.
A side stripper 3 is added to realize the separation of NH3, CO2 and H2S in one tower, CO2 and H2S are discharged from the top of the tower, ammonia gas is extracted from the middle part of the tower, a plurality of gas phase outlets are arranged in the middle part of the stripper 3, and different side-draw outlets of ammonia-containing steam can be selected according to different material components or process requirements;
a secondary cooling feeding system is added, a section of washing filler is added at the top of the stripping tower 3, and ammonia in the acid gas is removed through desalted water or clean process water washing absorption, so that the problem that the pipeline is blocked due to the crystallization of ammonium salt formed by the acid gas and the ammonia in a post system is prevented, and the loss and waste of ammonia resources and the problem of environmental protection caused by the loss and the waste of the ammonia resources are also avoided;
an acid gas heating system is added, an acid separator 6 is arranged on an acid gas pipeline at the top of the stripping tower 3, the acid gas with water separated is heated by low-pressure steam to form a supersaturated state, and the acid gas is prevented from being cooled and condensed in the pipeline conveying process, so that the acid gas and ammonia gas are prevented from forming ammonium salt crystals to block the pipeline;
and a three-stage cooling and dephlegmating system is added, most of the acid gas is removed from the stripping tower, and the rest of the acid gas is fixed in the separating liquid by ammonia gas in the step-by-step cooling process, so that high-purity ammonia gas is obtained.
Claims (2)1. A coking wastewater ammonia distillation treatment device comprises a raw material water tank (1), a raw material water pump (2), a stripping tower (3), a reboiler (4), a feeding cooler (5), an acid separator (6), a purification water pump (7), a secondary preheater (8), a primary preheater (9), a primary dephlegmator (10), a secondary condenser (11), a secondary dephlegmator (12), a tertiary condenser (13), a tertiary dephlegmator (14) and a dephlegmator cooler (15);
the method is characterized in that: the bottom of the raw material water tank (1) is divided into two paths through a raw material water pump (2), one path is connected with the middle upper part of the stripping tower (3) through a feeding cooler (5), and the other path is connected with the middle part of the stripping tower (3) through a primary preheater (9) and a secondary preheater (8) in sequence;
the top end of the stripping tower (3) is connected with an acid separator (6), the middle part of the stripping tower (3) is connected with a primary dephlegmator (10) through a primary preheater (9), one end of the bottom of the stripping tower (3) is connected with a secondary preheater (8) through a purification water pump (7), and the other end of the bottom of the stripping tower (3) is connected with the bottom of the stripping tower (3) through a reboiler (4);
the bottom end of the acid separator (6) is connected with the middle part of the raw material water tank (1);
the top of the first-stage dephlegmator (10) is connected with the middle of a second-stage dephlegmator (12) through a second-stage condenser (11), and the top of the second-stage dephlegmator (12) is connected with a third-stage dephlegmator (14) through a third-stage condenser (13);
the bottom of the first-stage partial condenser (10) and the bottom of the second-stage partial condenser (12) are communicated with the bottom of the third-stage partial condenser (14) through a condensate cooler (15) and then are connected to the middle part of the raw material water tank (1).
2. The coking wastewater ammonia distillation treatment device of claim 1, which is characterized in that: the low-pressure steam passes through an acid separator (6) to remove steam condensate.
CN202221434542.6U 2022-06-10 2022-06-10 Coking wastewater ammonia distillation treatment device Active CN217458889U (en) Priority Applications (1) Application Number Priority Date Filing Date Title CN202221434542.6U CN217458889U (en) 2022-06-10 2022-06-10 Coking wastewater ammonia distillation treatment device Applications Claiming Priority (1) Application Number Priority Date Filing Date Title CN202221434542.6U CN217458889U (en) 2022-06-10 2022-06-10 Coking wastewater ammonia distillation treatment device Publications (1) Family ID=83235269 Family Applications (1) Application Number Title Priority Date Filing Date CN202221434542.6U Active CN217458889U (en) 2022-06-10 2022-06-10 Coking wastewater ammonia distillation treatment device Country Status (1)RetroSearch is an open source project built by @garambo | Open a GitHub Issue
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