CN114147030A - Direct exhaust tail gas recycling system for nylon 66 continuous polycondensation device - Google Patents
Direct exhaust tail gas recycling system for nylon 66 continuous polycondensation device Download PDFInfo
- Publication number
- CN114147030A CN114147030A CN202111409610.3A CN202111409610A CN114147030A CN 114147030 A CN114147030 A CN 114147030A CN 202111409610 A CN202111409610 A CN 202111409610A CN 114147030 A CN114147030 A CN 114147030A
- Authority
- CN
- China
- Prior art keywords
- steam
- outlet pipe
- nylon
- tank
- saturation tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B08—CLEANING
- B08B—CLEANING IN GENERAL; PREVENTION OF FOULING IN GENERAL
- B08B15/00—Preventing escape of dirt or fumes from the area where they are produced; Collecting or removing dirt or fumes from that area
- B08B15/04—Preventing escape of dirt or fumes from the area where they are produced; Collecting or removing dirt or fumes from that area from a small area, e.g. a tool
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G69/00—Macromolecular compounds obtained by reactions forming a carboxylic amide link in the main chain of the macromolecule
- C08G69/02—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids
- C08G69/26—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids derived from polyamines and polycarboxylic acids
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G69/00—Macromolecular compounds obtained by reactions forming a carboxylic amide link in the main chain of the macromolecule
- C08G69/02—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids
- C08G69/26—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids derived from polyamines and polycarboxylic acids
- C08G69/28—Preparatory processes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G5/00—Controlling superheat temperature
- F22G5/12—Controlling superheat temperature by attemperating the superheated steam, e.g. by injected water sprays
- F22G5/123—Water injection apparatus
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/00033—Continuous processes
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Polyamides (AREA)
Abstract
The invention belongs to the technical field of nylon 66 production, and particularly relates to a recycling system for direct exhaust steam of a nylon 66 continuous polycondensation device. The system comprises a nylon 66 continuous polymerization reactor, wherein the nylon 66 continuous polymerization reactor is connected with a steam saturation tower through a steam pipeline, the steam saturation tower is connected with a filter through a steam pipeline, the steam saturation tower is connected with a solution recovery tank through a waste liquid pipe, and the filter is also connected with a concentration tank through a steam pipeline; the solution recovery tank is also connected with a desalted water replenishing pipe and a water outlet pipe, the water outlet pipe comprises a first water outlet pipe and a second water outlet pipe, the first water outlet pipe is connected with the steam saturation tower, and the second water outlet pipe is connected with the solution storage tank. The method recovers the hexamethylene diamine in the steam as much as possible when recovering the exhaust heat energy of the polymerization reactor, reduces the discharge of the hexamethylene diamine, oligomers and impurities easy to scale and equipment blockage, has little discharge of three wastes, and meets the requirements of energy conservation, emission reduction and environmental protection in the continuous polymerization melt direct spinning production process of nylon 66.
Description
Technical Field
The invention belongs to the technical field of nylon 66 production, and particularly relates to a recycling system for direct exhaust steam of a nylon 66 continuous polycondensation device.
Background
In the continuous polymerization melt direct spinning production process of nylon 66, a large amount of superheated steam is discharged from a reactor under the conditions of 1.80-1.85 MPa and 235-270 ℃, the superheated steam contains trace amounts of hexamethylenediamine and oligomer, and in the prior art, most of the superheated steam is directly discharged into the atmosphere as tail steam. In addition, in the continuous polymerization process, not only 50% of solvent water needs to be completely evaporated, but also water generated in the polycondensation reaction needs to be evaporated to prepare the polymer with the molecular weight stably controlled within 29000-30000, and a large amount of heat is wasted in the process.
Therefore, the full recycling of the waste heat of the tail gas of the polymerization reactor is one of the necessary measures of energy conservation, emission reduction and environmental protection.
However, the hexamethylenediamine and the oligomers in the steam are slightly toxic substances, and if the hexamethylenediamine and the oligomers are discharged into the air, the environment is inevitably polluted. On the other hand, when the melting point of the hexamethylene diamine, the hexamethylene diamine oligomer and other impurities is lower than the melting point of the hexamethylene diamine oligomer and the hexamethylene diamine oligomer, the hexamethylene diamine oligomer and other impurities can be condensed and crystallized, form dirt during long-term operation, are adhered to the wall surface, and easily block equipment and pipelines, so that the heat exchange efficiency of the equipment is reduced, even the production is stopped, and larger loss is caused. Therefore, how to remove the impurities which are easy to scale in the steam is a problem which must be considered when the steam is recovered.
Disclosure of Invention
The invention provides a recycling system for continuous direct exhaust tail gas of nylon 66, which aims to realize the purposes of recycling hexamethylene diamine in steam as much as possible and reducing the discharge of hexamethylene diamine, oligomers and impurities easy to scale and equipment blockage when recycling exhaust heat energy of a polymerization reactor, and meets the requirements of energy conservation, emission reduction and environmental protection in the production process of continuous polymerization melt direct spinning of nylon 66.
In order to achieve the purpose, the technical scheme of the invention is as follows:
a recycling system of continuous direct exhaust tail gas is connected with a nylon 66 continuous polymerization reactor, specifically, the nylon 66 continuous polymerization reactor is connected with a steam saturation tower through a steam pipeline, the steam saturation tower is connected with a filter through the steam pipeline, the steam saturation tower is connected with a solution recycling tank through a waste liquid pipe, and the filter is also connected with a concentration tank through the steam pipeline;
the solution recovery tank is also connected with a desalted water replenishing pipe and a water outlet pipe, the water outlet pipe comprises a first water outlet pipe and a second water outlet pipe, the first water outlet pipe is connected with the steam saturation tower, and the second water outlet pipe is connected with the solution storage tank.
In a further optimized scheme, the nylon 66 continuous polymerization reactor is connected with the lower part of the steam saturation tower through a steam pipeline, and the first water outlet pipe is connected with the upper part of the steam saturation tower. Furthermore, the first water outlet pipe extends into the upper part of the steam saturation tower and is connected with a spraying system, superheated steam rises to be fully mixed with desalted water, and the degree of superheat of the steam is reduced.
In a further optimization scheme, the spraying system is a water distributor, the height of the steam saturation tower is 10 meters, the lower part of the tower body is provided with the steam distributor, and a plurality of layers of metal corrugated plate packing are arranged in the tower body.
In a further optimization scheme, the top of the steam saturation tower is connected with the lower part of the filter through a steam pipeline, the bottom of the steam saturation tower is connected with the solution recovery tank through a waste liquid pipe, and the top of the filter is also connected with the concentration tank through a steam pipeline. The concentration tank is a concentration tank in a nylon 66 continuous polymerization reaction system. The concentration tank is a vertical cylindrical stirring tank with a jacket and a coil, and the prior art is to heat and concentrate salt liquid (nylon 66 salt water solution) by a heat medium through the coil to concentrate the concentration of the salt liquid from 50 percent to the range specified by the process.
In a further optimized scheme, a filter screen is arranged in the solution recovery tank and is used for removing oligomers in the waste liquid from the steam saturation tower; and a coil pipe is further arranged in one side of the filter screen of the solution recovery tank, the temperature of the filtered waste liquid is reduced to 20-30 ℃ by using circulating cooling water for recycling of the steam saturation tower, or the waste liquid containing the hexamethylene diamine is conveyed to a solution storage tank through a pipeline. A set of heating device is installed in the solution storage tank, and the temperature in the storage tank is kept at about 40-70 ℃ through a heat source, so that crystallization of hexamethylene diamine is avoided.
In a further optimized scheme, the steam saturation tower, the solution recovery tank and the solution storage tank are all connected with sewage pipes, and the sewage pipes are connected with a sewage treatment system. Wherein the sewage pipe of the steam saturation tower is positioned on the waste liquid pipe between the steam saturation tower and the solution recovery tank.
In a further optimization scheme, the bottom of the filter is also connected with a solution storage tank through a pipeline.
Through the technical scheme, the invention has the beneficial effects that:
the invention adopts a direct contact type temperature and pressure reduction mode of desalted water and superheated steam to recover the waste heat of the superheated steam. Pure medium pressure steam (pressure grade of 1.18 MPa) can be recovered in the recycling system, wherein the content of the hexamethylene diamine is in ppm level, and the oligomer is basically removed in a filter. The waste liquid rich in hexamethylene diamine generated by the system can be intensively recycled.
The invention has less discharge of three wastes, and a very small amount of low-pressure waste steam has no toxic substances, meets the requirement of environmental protection, and can be directly discharged. The hexanediamine waste liquid can be intensively recycled into the measuring tank and can be sold after reaching a certain amount. The system has no waste slag discharge.
Drawings
FIG. 1 is a schematic structural diagram of a nylon 66 continuous polymerization reaction system.
FIG. 2 is a schematic structural diagram of a continuous direct exhaust steam recycling system according to the present invention.
The reference numbers in the drawings are as follows: 01 is a metering tank, 02 is an intermediate tank, 03 is a salt filter, 04 is a concentration tank, 05 is a preheater, 06 is a reactor, 07 is a decompressor, 08 is a front polymerizer, and 09 is a rear polymerizer;
1 is a steam saturation tower, 11 is a spraying system, 12 is a waste liquid pipe, 2 is a filter, 3 is a solution recovery tank, 31 is a desalted water replenishing pipe, 321 is a first water outlet pipe, 322 is a second water outlet pipe, 33 is a filter screen, 34 is a coil pipe, 4 is a solution storage tank, and 5 is a sewage pipe.
Detailed Description
The invention is further described with reference to the following figures and detailed description:
the continuous polymerization production system of nylon 66 comprises a metering tank 01, an intermediate tank 02, a salt filter 03, a concentration tank 04, a preheater 05, a reactor 06, a pressure reducer 07, a pre-polymerizer 08 and a post-polymerizer 09 which are connected in sequence. The nylon 66 continuous polymerization uses 50% wt nylon 66 salt solution, the 50% wt nylon 66 salt solution is firstly filtered to remove impurities in the salt solution and then conveyed to the metering tank 01 in batches, and a certain amount of heat stabilizer is accurately added into the metering tank 01 and uniformly mixed; the salt solution mixture is added in portions to an intermediate tank 02 provided below the metering tank 01. Then, the salt is supplied to the salt filter 03 by the salt supply pump to remove impurities again, and the salt is preheated and continuously supplied to the concentration tank 04. The salt solution from the concentration tank 04 is heated by a preheater 05 and then enters the reactor 06 for reaction. Under the conditions of 1.85MPa and 235-270 ℃, materials in the reactor 06 are subjected to pre-polycondensation, and evaporated superheated steam is directly discharged into the atmosphere. And then the material enters a pressure reducer 07, the pressure reducer 07 reduces the pressure of the material outlet from 2.0-3.0 MPa to the normal pressure, and simultaneously, the temperature of the prepolymer is increased to 280-300 ℃. The prepolymer after being heated sequentially enters a front polymerizer 08 and a rear polymerizer 09 for polymerization reaction, so that the relative viscosity of the polymer meets the requirements of the spinning process, and then the polymer is conveyed to the spinning process through a pressurizing conveying pump.
The recycling system of tail gas in direct row of this embodiment is connected with nylon 66 continuous polymerization reactor 06, specifically, nylon 66 continuous polymerization reactor 06 passes through the steam conduit and connects steam saturation tower 1 lower part, and steam saturation tower 1 top passes through the steam conduit and connects filter 2 lower part, and steam saturation tower 1 bottom passes through waste liquid pipe 12 and connects solution recovery tank 3.
The top of the filter 2 is also connected with a concentration tank 4 through a steam pipeline, and oligomers contained in medium-pressure steam from the steam saturation tower 1 are removed in the filter 2, so that the oligomers are prevented from accumulating in the concentration tank 04 to block a coil. In this embodiment, the filter 2 has two sets, one set for use and one set for standby, and the filter 2 is internally provided with a pressure control device, and when the pressure drop reaches a certain amount, the filter 2 is controlled to be closed through a valve, and the filter 2 for standby is started. The filler in the filter 2 can be taken out and can be recycled after heat treatment. The concentration tank 04 is the concentration tank 04 in the nylon 66 continuous polymerization reaction system. The concentration tank 04 is a vertical cylindrical stirring tank with a jacket and a coil, and the prior art is that salt liquid (nylon 66 salt water solution) is heated and concentrated by a heating medium through the coil, and the bottom of the filter 2 is also connected with a solution storage tank 4 through a pipeline.
The solution recovery tank 3 is also connected with a desalted water replenishing pipe 31 and a water outlet pipe, the water outlet pipe comprises a first water outlet pipe 321 and a second water outlet pipe 322, the first water outlet pipe 321 is connected with the upper part of the steam saturation tower 1, the first water outlet pipe 321 extends into the upper part of the steam saturation tower 1 and is connected with a spraying system 11, superheated steam rises to be fully mixed with desalted water, and the degree of superheat of the steam is reduced. The second outlet pipe 322 is connected to the solution tank 4.
A filter screen 33 is installed in the solution recovery tank 3 near the inlet of the waste liquid pipe 12, and oligomers in the waste liquid from the steam saturation tower 1 are removed through the filter screen 33; a coil pipe 34 is further installed in one side of the filter screen 33, the temperature of the filtered waste liquid is reduced to 20-30 ℃ by using circulating cooling water, and then the waste liquid is recycled by the steam saturation tower 1 through a first water outlet pipe 321, or the waste liquid containing the hexamethylene diamine is conveyed to the solution storage tank 4 through a pipeline. A set of heating pipelines is arranged in the solution storage tank 4, and the temperature in the solution storage tank 4 is kept at about 40-70 ℃ by a heat source (steam) so as to avoid crystallization of hexamethylene diamine.
The steam saturation tower 1, the solution recovery tank 3 and the solution storage tank 4 are all connected with a sewage pipe 5, and the sewage pipe 5 is connected with a sewage treatment system. Wherein the sewer pipe 5 of the steam saturation tower 1 is located on the waste liquid pipe 12 between the steam saturation tower 4 and the solution recovering tank 3.
Wherein, the height of the steam saturation tower 1 is 10 meters, so as to ensure the retention time of the superheated steam in the tower; the lower part of the tower body is provided with a gas distributor, so that the gas is uniformly distributed in the saturation tower; the interior of the tower body is provided with a plurality of layers of metal corrugated plate packing to replace the original ceramic pall ring packing, so that the contact area of superheated steam and spray water is increased; the spraying system 11 at the upper part of the tower body is a water distributor, so that superheated steam and spray water are fully mixed, the degree of superheat is reduced, and secondary polymerization and deposition of oligomers are avoided. The capacity of the steam saturation tower 1 for treating superheated steam is 1200-1900 kg/h, the pressure of recovered saturated steam is stably controlled to be 0.8-0.9 MPa, the content of hexamethylene diamine is less than or equal to 100ppm, the outlet pipeline of the saturation tower, an adjusting valve and a steam inlet adjusting valve of a concentration tank are not blocked, the steam saturation tower can stably run for 18-20 months, and the steam saturation tower can well run.
When in use, firstly, superheated steam generated in the reactor 06 of the chinlon 66 continuous polymerization production system enters from the bottom of the steam saturation tower 1 and flows upwards; then normal temperature desalted water is sprayed into the tower in a fog shape from a spraying system 11 at the top of the tower, namely an anti-blocking nozzle of a water distributor, and is fully contacted with superheated steam, the superheated steam is rapidly cooled into medium pressure saturated steam by utilizing the larger heat transfer rate between the desalted water and the superheated steam, the medium pressure saturated steam enters a filter 2 through a steam pipeline, regular packing is filled in the filter 2, oligomer impurities in the saturated steam are removed through the filter 2, and pure medium pressure steam is prepared to be used as a heat source of a concentration tank 04 to replace the original heat medium.
The low-pressure steam generated by the steam saturation tower 1 can be discharged through a low-pressure steam pipeline connected to the top.
In addition, the hexamethylenediamine in the superheated steam is washed in the steam saturation tower 1, a hexamethylenediamine-rich waste liquid is formed at an overflow port at the bottom of the steam saturation tower 1, the hexamethylenediamine-rich waste liquid flows through a drain valve through a waste liquid pipe 12 to the solution recovery tank 3, and then the hexamethylenediamine-rich waste liquid is filtered by a filter screen 33 and cooled by a coil pipe 34 in the solution recovery tank 3 to be recycled by the steam saturation tower 1 so as to continuously enrich the hexamethylenediamine solution. When the solution processed by the solution recycling tank 3 meets the requirement, the solution can be transported to the solution storage tank 4 through the second outlet pipe 322. This realizes the concentration and recovery of hexamethylenediamine in the superheated steam, wherein trace hexamethylenediamine and low molecular polymer in the steam saturation tower 1 and the solution storage tank 4 are discharged into a sewage treatment system along with the condensed water for biochemical treatment.
Furthermore, the condensed water produced by the filter 2 may enter the solution reservoir 4.
After the recycling system is used, superheated steam with the pressure of 18.5 MPa and the temperature of 235-270 ℃ from a reactor can be treated into medium-pressure steam with the pressure of 1.18MPa, and hexamethylene diamine in the superheated steam is recycled, so that low polymers and other easily-scaling impurities in the superheated steam are removed. The safety production is the key of a chemical device, and two sets of safety valves are arranged at the top of a saturated steam tower in order to prevent a tower system and other devices from being overpressured. And in the accident state, the safety valve is opened and is discharged to a safety place.
The above-described embodiments are merely preferred embodiments of the present invention, and not intended to limit the scope of the invention, so that equivalent changes or modifications in the structure, features and principles described in the present invention should be included in the claims of the present invention.
Claims (7)
1. A recycling system of continuous direct exhaust tail gas comprises a nylon 66 continuous polymerization reactor (06), and is characterized in that the nylon 66 continuous polymerization reactor (06) is connected with a steam saturation tower (1) through a steam pipeline, the steam saturation tower (1) is connected with a filter (2) through a steam pipeline and is connected with a solution recycling tank (3) through a waste liquid pipe, and the filter (2) is also connected with a concentration tank (04) through a steam pipeline;
still be connected with desalinized water moisturizing pipe (31) and outlet pipe on solution recovery tank (3), the outlet pipe includes first outlet pipe (321) and second outlet pipe (322), and steam saturation tower (1) is connected in first outlet pipe (321), and solution storage tank (4) is connected in second outlet pipe (322).
2. The recycling system of the continuous direct exhaust steam according to claim 1, characterized in that the nylon 66 continuous polymerization reactor (06) is connected with the lower part of the steam saturation tower (1) through a steam pipeline, and the first water outlet pipe (321) extends into the upper part of the steam saturation tower (1) and is connected with the spraying system (11).
3. The recycling system of continuous direct exhaust tail gas according to claim 2, characterized in that the spraying system (11) is a water distributor, the height of the steam saturation tower (1) is 10 m, the lower part of the tower body is provided with a steam distributor, and the tower body is internally provided with a plurality of layers of metal corrugated plate packing.
4. The recycling system of continuous direct exhaust tail gas as claimed in claim 1, wherein the top of the steam saturation tower (1) is connected with the lower part of the filter (2) through a steam pipeline, the bottom of the steam saturation tower (1) is connected with the solution recycling tank (3) through a waste liquid pipe (12), and the top of the filter (2) is also connected with the concentration tank (04) through a steam pipeline.
5. The recycling system of continuous direct exhaust tail gas according to claim 1, characterized in that a filter screen (33) is installed in the solution recycling tank (3), and a coil (34) is installed in one side of the filter screen (33); and a set of heating device is arranged in the solution storage tank (4).
6. The recycling system of continuous direct exhaust tail gas according to claim 1, characterized in that the steam saturation tower (1), the solution recovery tank (3) and the solution storage tank (4) are connected with a sewage pipe (5), and the sewage pipe (5) is connected with a sewage treatment system; wherein the sewage pipe (5) of the steam saturation tower (1) is positioned on the waste liquid pipe (12) between the steam saturation tower (1) and the solution recovery tank (3).
7. A recycling system for continuous direct exhaust tail gas according to claim 1, characterized in that the bottom of the filter (2) is connected with the solution storage tank (4) through a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111409610.3A CN114147030A (en) | 2021-11-23 | 2021-11-23 | Direct exhaust tail gas recycling system for nylon 66 continuous polycondensation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111409610.3A CN114147030A (en) | 2021-11-23 | 2021-11-23 | Direct exhaust tail gas recycling system for nylon 66 continuous polycondensation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114147030A true CN114147030A (en) | 2022-03-08 |
Family
ID=80457775
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111409610.3A Pending CN114147030A (en) | 2021-11-23 | 2021-11-23 | Direct exhaust tail gas recycling system for nylon 66 continuous polycondensation device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114147030A (en) |
-
2021
- 2021-11-23 CN CN202111409610.3A patent/CN114147030A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101318752B (en) | Treatment method and apparatus for recycling ammonia nitrogen wastewater | |
| CN101367507B (en) | Gas removing, filtering and extracting method for waste sulphuric acid | |
| CN110054164B (en) | Concentrated recovery system of dilute sulfuric acid | |
| CN103391898A (en) | Method for recycling deoiled water using counterflow falling-film evaporators | |
| CN101445290A (en) | Environment-friendly high-performance waste water ammonia-removal process and device thereof | |
| CN109704492B (en) | Harmless resourceful treatment system of waste salt | |
| CN107117755A (en) | A kind of high ammonia-nitrogen wastewater processing and ammonia recovery system and its method | |
| CN212269507U (en) | High-concentration wastewater zero discharge system for blast furnace slag flushing cleaning production and waste heat method in steel plant | |
| CN101200423A (en) | Epoxy ester wastewater recycling treatment method | |
| CN111847744B (en) | System and method for treating high-salt organic wastewater in ion exchange resin production | |
| CN102557317A (en) | Zero-discharge treatment process for salt-containing waste water | |
| CN103342435A (en) | Comprehensive utilization device of acetylene purification waste sodium hypochlorite | |
| CN108117208A (en) | The processing method and processing unit of a kind of alkali residue waste liquid | |
| CN216631989U (en) | A recycle system that is used for direct vent tail gas of nylon 66 continuous polycondensation device | |
| CN111470694A (en) | Zero-discharge reclaimed water recycling process and system for pharmaceutical wastewater | |
| CN114147030A (en) | Direct exhaust tail gas recycling system for nylon 66 continuous polycondensation device | |
| CN206033465U (en) | Coal chemical wastewater preliminary treatment deamination system | |
| CN104098214B (en) | Containing wastewater from catalyst treatment system | |
| CN206705701U (en) | A kind of high ammonia-nitrogen wastewater processing and ammonia recovery system | |
| CN210302462U (en) | Stable and continuous operation's anticorrosion petroleum resin flash distillation system | |
| CN104696946A (en) | Process and process system for steam exhaust liquid heat energy recovery and desalted water recovery | |
| CN114735876A (en) | System and method for reducing organic silicon wastewater treatment energy consumption by utilizing waste heat | |
| KR20040096077A (en) | the Device for Cleaning Sewage | |
| CN114604980A (en) | Raw water heating and hard water removing treatment device | |
| CN106051704A (en) | System for recovering high temperature coal gas waste heat with molten salt |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |