CN211972044U - Surplus aqueous ammonia processing apparatus in coking process - Google Patents
Surplus aqueous ammonia processing apparatus in coking process Download PDFInfo
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- CN211972044U CN211972044U CN202020360328.5U CN202020360328U CN211972044U CN 211972044 U CN211972044 U CN 211972044U CN 202020360328 U CN202020360328 U CN 202020360328U CN 211972044 U CN211972044 U CN 211972044U
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Abstract
The utility model belongs to the technical field of surplus aqueous ammonia processing apparatus, a surplus aqueous ammonia processing apparatus in coking process is disclosed, including ammonia still and heat exchanger. The water discharge pipe mouth of the ammonia still is connected with the liquid inlet of the cyclone separator through a pipeline, and the cyclone separator is used for separating water liquid and tar in oil-water mixed liquid discharged from the ammonia still. The leakage fluid dram of cyclone has the subsider through the pipe connection, the subsider is used for buffering the water liquid of cyclone separation ware separation and subsides the separation, still be equipped with first water pump on the pipeline between the tube side of subsider and heat exchanger, first water pump carries the clear liquid in the subsider to the heat exchanger in, and the oil drain port of subsider bottom is connected with the tar processing apparatus of chemical product, the tar processing apparatus of chemical product is handled the discharged tar sediment of subsider, the subsider is used for subsiding the separation to the water liquid of cyclone separation ware separation. The residual ammonia water treatment device has the advantages of high efficiency, simplicity and energy conservation, and can avoid the influence on the heat exchange effect caused by the blockage of the heat exchanger.
Description
Technical Field
The utility model belongs to the technical field of surplus aqueous ammonia processing apparatus, concretely relates to surplus aqueous ammonia processing apparatus in coking process.
Background
A large amount of residual ammonia water is generated in the coking process of a coking plant, contains toxic and harmful substances such as ammonia, phenol, sulfide, cyanide, pyridine, coal tar and the like, and is a main source of industrial sewage in a coking process.
The residual ammonia water is generally sent to a biochemical treatment system for treatment after being subjected to heat exchange by a heat exchanger after being partially recycled by an ammonia still. Because the ammonia wastewater after the residual ammonia water passes through the ammonia still has high temperature and large oil content, when the residual ammonia water is cooled by the heat exchanger, tar in the residual ammonia water discharged by the ammonia still is cooled and then easily blocks the heat exchanger, so that the heat exchange effect of the heat exchanger is reduced, the heat exchanger needs to be cleaned and maintained after long-term operation, and the heat exchanger is frequently maintained, so that the production can be stopped and the normal production is influenced; on the other hand, the heat exchanger overhauls and to increase intensity of labour, and frequently overhauls and to reduce the life of heat exchanger for device use cost risees by a wide margin.
Therefore, there is a need for an improvement in the existing apparatus for treating residual ammonia water.
Disclosure of Invention
An object of the utility model is to solve the heat exchanger and be blockked up easily among the current surplus aqueous ammonia processing apparatus, cause reduction, the increase of operation intensity of labour, the increase of device cost, the extension scheduling problem of surplus aqueous ammonia processing cycle of surplus aqueous ammonia treatment effeciency, provide a surplus aqueous ammonia processing apparatus in high-efficient, simple, energy-conserving coking process.
Realize the utility model discloses the technical scheme of purpose as follows: the device comprises an ammonia still and a heat exchanger, wherein the ammonia still is used for recovering the residual ammonia water in the coking process, and the treated residual ammonia water discharged by the ammonia still enters a biochemical process for treatment after the water discharged by the heat exchanger for heat exchange. The water discharge pipe mouth of the ammonia still is connected with the liquid inlet of the cyclone separator through a pipeline, and the cyclone separator is used for separating water liquid and tar in oil-water mixed liquid discharged from the ammonia still.
The drain outlet of cyclone is connected with the subsider through the pipeline, still is equipped with first water pump on the pipeline between the tube side of subsider and heat exchanger, and the oil drain port of subsider bottom is connected with the tar processing apparatus of chemical product, and the subsider is used for settling the separation to the water liquid of cyclone separation.
The cyclone separator is arranged between the ammonia still and the heat exchanger, so that an oil-water mixture discharged from the ammonia still can be separated, and part of tar in the oil-water mixture is separated, thereby avoiding the heat exchanger from being blocked and influencing the heat exchange effect. Meanwhile, the rear end of the cyclone separator is connected with a settling tank, the settling tank can settle the oil-water mixture discharged by the cyclone separator, further tar in the oil-water mixture is separated again, the proportion of the tar in the oil-water mixture entering the heat exchanger is reduced again, the heat exchange effect of the heat exchanger is ensured, and the normal operation of equipment is ensured.
As right the utility model discloses an improve, because the temperature through ammonia still exhaust oil-water mixed liquid is about 107~113 ℃, in order to carry out abundant recovery with the remaining ammonia in the ammonia still exhaust oil-water mixed liquid to make full use of oil-water mixed liquid's heat makes surplus ammonia water treatment facilities still include the flash tank, and the drain pipe mouth of pipe of flash tank and ammonia still is connected through the pipeline, the gas vent on flash tank upper portion and ammonia still's access connection.
In order to facilitate smooth conveying of oil-water mixed liquid in a flash tank at the bottom of the flash tank to the cyclone separator, a liquid outlet of the flash tank is connected with a liquid inlet of the cyclone separator, and a second water pump is arranged between the flash tank and the cyclone separator.
As right the utility model discloses an it is right that the improvement still is equipped with heat transfer and pressure device on the air inlet pipeline of flash tank upper portion gas vent and ammonia still, and heat transfer and pressure device can be adjusted the gas that gets into the ammonia still through the flash tank, make it can be handled better and recycle.
As right the utility model discloses an it is right to improve, still twine the cooling water pipe on the periphery wall of subsider, the play water end of cooling water pipe and steam production preprocessing device's entrance connection. The setting of cooling water pipe can slow down the pressure of heat exchanger, ensures the cooling effect of oil-water mixture liquid, simultaneously, will cool down the play water end of water pipe and steam production preprocessing device's entrance connection, can make full use of oil-water mixture liquid's heat energy, carries out rational utilization with heat energy, can reduce steam production preprocessing device's cost.
Furthermore, in order to reduce the possibility of overhauling of the heat exchanger due to the blockage of tar impurities as much as possible, the service life of the heat exchanger is prolonged, a small amount of precipitated tar is prevented from being sucked into the heat exchanger by the first water pump, the first water pump or the tube side of the heat exchanger is blocked, and a filter is further arranged between the settling tank and the first water pump.
As right the utility model discloses an it is right to improve, in order to implement the heat transfer effect of control heat exchanger, ensures to be sent to the temperature of the waste water of changing the product tar processing apparatus, avoids changing the activity of the strain of producing tar processing apparatus because of the too high influence of exhaust waste water temperature, is equipped with temperature measuring device respectively at the front end of the tube side of heat exchanger and rear end.
Furthermore, the front end of the tube pass of the heat exchanger is also provided with a flow regulating electromagnetic valve, and the temperature measuring device and the flow regulating electromagnetic valve are electrically connected with the controller. The water temperatures of the front end and the rear end of the heat exchanger are measured by the temperature measuring device, and the flow of the flow regulating electromagnetic valve is controlled and regulated in time by the controller, so that the temperature of the wastewater sent to the chemical tar production treatment device is further ensured.
Compared with the prior art, the beneficial effects of the utility model are that: through improving the surplus aqueous ammonia processing apparatus in the coking process that has now, increase cyclone, subsider between ammonia still and heat exchanger, can in time separate the tar in the oily water mixture liquid of surplus aqueous ammonia to reduce and avoid the condition that the heat exchanger is blockked up even, ensured the heat transfer effect of heat exchanger, reduce the heat exchanger and overhaul the number of times.
Drawings
FIG. 1 is a schematic view of a residual ammonia water treatment apparatus according to the present invention;
wherein, 1, an ammonia still; 2. a heat exchanger; 3. a cyclone separator; 4. a settling tank; 5. a first water pump; 6. a flash tank; 7. a second water pump; 8. a filter; 9. a heat exchange and pressurization device.
Detailed Description
The present invention is described in detail with reference to the embodiments shown in the drawings, but it should be understood that these embodiments are not intended to limit the present invention, and those skilled in the art should understand that the functions, methods, or structural equivalents or substitutions made by these embodiments are within the scope of the present invention.
In the description of the present embodiments, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of describing the present invention and simplifying the description, but do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," "third," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicit to a number of indicated technical features. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the invention, the meaning of "a plurality" is two or more unless otherwise specified.
The terms "mounted," "connected," and "coupled" are to be construed broadly and may, for example, be fixedly coupled, detachably coupled, or integrally coupled; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the creation of the present invention can be understood by those of ordinary skill in the art through specific situations.
Example 1:
referring to fig. 1, a residual ammonia water treatment apparatus in a coking process includes an ammonia still 1 and a heat exchanger 2 in the present embodiment. The water discharge pipe mouth of the ammonia still 1 is connected with the liquid inlet of the cyclone separator 3 through a pipeline, and the cyclone separator 3 is used for separating water liquid and tar in the oil-water mixed liquid discharged from the ammonia still 1.
The drain outlet of cyclone 3 is connected with a settling tank 4 through a pipeline, a first water pump 5 is arranged on the pipeline between the settling tank 4 and the tube side of the heat exchanger 2, an oil outlet at the bottom of the settling tank 4 is connected with a chemical product tar treatment device, and the settling tank 4 is used for settling and separating the water liquid separated by the cyclone 3.
Be equipped with cyclone 3 between ammonia still 1 and heat exchanger 2, can separate through ammonia still 1 exhaust water oil mixture, make partial tar in the water oil mixture separate to avoided heat exchanger 2 to be blockked up, influenced heat transfer effect.
The rear end of the cyclone separator 3 is connected with a settling tank 4, the settling tank 4 can settle the oil-water mixture discharged from the cyclone separator 3, further tar in the oil-water mixture is separated again, the proportion of the tar in the oil-water mixture entering the heat exchanger 2 is reduced again, the heat exchange effect of the heat exchanger is ensured, and the normal operation of the equipment is ensured.
The residual ammonia water treatment device operates, wherein the concentration of ammonia water recovered and discharged from the top of the ammonia still 1 is about 10-15%, tar discharged from the bottom of the ammonia still 1 is about 5-7% of the total amount of tar in the oil-water mixture, and the ammonia water recovered from the ammonia still 1 is 60-70% of the total amount of ammonia in the oil-water mixture; the tar discharged by the cyclone separator 3 is about 30-40% of the total tar in the oil-water mixture; the tar discharged from the settling tank 4 is about 15-20% of the total tar in the oil-water mixture; the tar discharged from the ammonia still 1, the cyclone separator 3 and the settling tank 4 is input into the tar residue treatment device to be treated, and the ammonia still 1, the cyclone separator 3 and the settling tank 4 treat about 30-62% of the total tar content in the oil-water mixture, so that the tar content in the oil-water mixture is greatly reduced, the blockage of the heat exchanger 2 is avoided, and the heat exchange effect of the heat exchanger 2 is ensured.
Example 2:
referring to fig. 1, a remaining ammonia water treatment apparatus in a coking process, in the present embodiment, includes an ammonia still 1 and a heat exchanger 2. The water discharge pipe mouth of the ammonia still 1 is connected with the liquid inlet of the cyclone separator 3 through a pipeline, and the cyclone separator 3 is used for separating water liquid and tar in the oil-water mixed liquid discharged from the ammonia still 1.
The drain outlet of cyclone 3 is connected with a settling tank 4 through a pipeline, a first water pump 5 is arranged on the pipeline between the settling tank 4 and the tube side of the heat exchanger 2, an oil outlet at the bottom of the settling tank 4 is connected with a chemical product tar treatment device, and the settling tank 4 is used for settling and separating the water liquid separated by the cyclone 3.
The temperature of the oil-water mixed liquid discharged from the ammonia still 1 is about 107-113 ℃, so that the residual ammonia in the oil-water mixed liquid discharged from the ammonia still 1 can be fully recovered, the heat of the oil-water mixed liquid can be fully utilized, a flash tank 6 is further arranged between the ammonia still 1 and the cyclone separator 3, specifically, the flash tank 6 is connected with a water discharge pipe opening of the ammonia still 1 through a pipeline, and an exhaust port at the upper part of the flash tank 6 is connected with an inlet of the ammonia still 1. The flash tank 6 recovers and fully utilizes heat energy and ammonia in the oil-water mixed liquid discharged from the ammonia still 1, and the temperature of the oil-water mixed liquid discharged from the flash tank 6 is reduced to 90-100 ℃ from 107-113 ℃.
Preferably, a heat exchange and pressurization device 9 is further arranged on an exhaust port at the upper part of the flash tank 6 and an air inlet pipeline of the ammonia still 1, and the heat exchange and pressurization device 9 can adjust the gas entering the ammonia still 1 through the flash tank 6, so that the gas can be better treated and reused.
In order to facilitate smooth conveying of oil-water mixed liquid in the flash tank at the bottom of the flash tank 6 to the cyclone separator 3, a liquid outlet of the flash tank 6 is connected with a liquid inlet of the cyclone separator 3, and a second water pump 7 is further arranged between the flash tank 6 and the cyclone separator 3.
As an improvement to the settling tank 4 of this embodiment, a cooling water pipe is further wound around the peripheral wall of the settling tank 4, and the water outlet end of the cooling water pipe is connected to the inlet end of the steam generating device. The setting of cooling water pipe can slow down the pressure of heat exchanger 2, ensures the cooling effect of oil-water mixture liquid, simultaneously, will cool down the play water end of water pipe and the entrance connection that steam produced preprocessing device, can make full use of oil-water mixture liquid's heat energy, carries out rational utilization with heat energy, can reduce steam and produce preprocessing device's cost. When surplus aqueous ammonia processing apparatus moves, the temperature that the subsider 4 can be with the water oil mixture who discharges from flash tank 6 reduces to 80~85 ℃ from 90~100 ℃, and its greatly reduced heat transfer pressure of heat exchanger 2, and further subside the tar in the water oil mixture in subsider 4, reduced the risk that heat exchanger 2 is blockked up more.
Further, in order to avoid that a small amount of precipitated tar in the settling tank 4 is sucked into the heat exchanger 2 by the first water pump 5 and the first water pump 5 or the tube side of the heat exchanger 2 is blocked, a filter 8 is further arranged between the settling tank 4 and the first water pump 5, the filter 8 can filter the oil-water mixture discharged from the settling tank 4, and the tar residues filtered and separated by the filter 8 enter the chemical tar production treatment device for recovery treatment.
As an improvement of the residual ammonia water treatment device of the embodiment, in order to monitor the heat exchange effect of the heat exchanger 2 and ensure the temperature of the wastewater sent to the chemical tar production treatment device, the temperature of the wastewater discharged by the heat exchanger 2 is reduced to below 40 ℃, so as to avoid the influence on the activity of strains of the chemical tar production treatment device due to the overhigh temperature of the discharged wastewater, temperature measuring devices (not shown in the drawing) are respectively arranged at the front end and the rear end of the tube pass of the heat exchanger 2.
Furthermore, the front end of the tube pass of the heat exchanger 2 is also provided with a flow regulating electromagnetic valve (not shown in the attached drawings), and the temperature measuring device and the flow regulating electromagnetic valve are electrically connected with the controller. The water temperatures of the front end and the rear end of the heat exchanger 2 are measured by the temperature measuring device, and the flow of the flow regulating electromagnetic valve is controlled and regulated in time by the controller, so that the temperature of the wastewater sent to the chemical tar production treatment device is further ensured.
Be equipped with cyclone 3 between ammonia still 1 and heat exchanger 2, can separate through ammonia still 1 exhaust water oil mixture, make partial tar in the water oil mixture separate to avoided heat exchanger 2 to be blockked up, influenced heat transfer effect.
Be connected with subsider 4 at cyclone 3's rear end to twine cooling water pipe on the outer wall of subsider 4, subsider 4 can subside and cool down cyclone 3 exhaust oil water mixture, and further separates the tar in the oil water mixture once more, reduces the proportion of tar in the oil water mixture that gets into heat exchanger 2 once more, ensures the heat transfer effect of heat exchanger, guarantees the normal operating of equipment.
A flash tank 6 is arranged between the ammonia still 1 and the cyclone separator 3, so that the heat energy in the oil-water mixture discharged from the ammonia still 1 can be fully utilized, and the tar in the oil-water mixture is further precipitated.
The residual ammonia water treatment device operates, wherein the concentration of ammonia water recovered and discharged from the top of the ammonia still 1 is about 10-15%, tar discharged from the bottom of the ammonia still 1 is about 5-7% of the total amount of tar in the oil-water mixture, and the ammonia water recovered from the ammonia still 1 is 80-85% of the total amount of ammonia in the oil-water mixture; the tar discharged by the flash tank 6 is about 16-20% of the total tar in the oil-water mixture, and the temperature of the discharged oil-water mixture is reduced to 90-100 ℃; the tar discharged by the cyclone separator 3 is about 25-30% of the total tar in the oil-water mixture; the tar discharged from the settling tank 4 is about 20-25% of the total tar in the oil-water mixture, and the temperature of the oil-water mixture discharged from the settling tank 4 is reduced to 80-85 ℃; after heat exchange is carried out by the heat exchanger 2, the temperature of the wastewater discharged by the heat exchanger 2 and sent to the chemical tar production treatment device is 30-35 ℃, the heat exchanger 2 is overhauled and cleaned once in 2-3 days before, and is overhauled once in 10-15 days after the device is improved.
The tar discharged from the ammonia still 1, the flash tank 6, the cyclone separator 3 and the settling tank 4 is input into a tar residue treatment device to be treated, and the four structures of the ammonia still 1, the flash tank 6, the cyclone separator 3 and the settling tank 4 are used for treating about 66-85% of the total tar content in the oil-water mixture, so that the tar content in the oil-water mixture is greatly reduced, the blockage of the heat exchanger 2 is avoided, and the heat exchange effect of the heat exchanger 2 is ensured.
The above list of details is only for the practical implementation of the present invention, and they are not intended to limit the scope of the present invention, and all equivalent implementations or modifications that do not depart from the technical spirit of the present invention should be included in the scope of the present invention.
It is obvious to a person skilled in the art that the invention is not restricted to details of the above-described exemplary embodiments, but that it can be implemented in other specific forms without departing from the spirit or essential characteristics of the invention. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Furthermore, it should be understood that although the present description refers to embodiments, not every embodiment may contain only a single embodiment, and such description is for clarity only, and those skilled in the art should integrate the description, and the embodiments may be combined as appropriate to form other embodiments understood by those skilled in the art.
Claims (7)
1. The utility model provides a surplus aqueous ammonia processing apparatus in coking process, includes ammonia still and heat exchanger, its characterized in that: a water discharge pipe orifice of the ammonia still is connected with a liquid inlet of a cyclone separator through a pipeline, and the cyclone separator is used for separating water liquid from tar in oil-water mixed liquid discharged by the ammonia still;
the liquid discharge outlet of the cyclone separator is connected with a settling tank through a pipeline, the settling tank and a first water pump are further arranged on the pipeline between the tube passes of the heat exchanger, an oil discharge outlet at the bottom of the settling tank is connected with a chemical product tar treatment device, and the settling tank is used for settling and separating the water liquid separated by the cyclone separator.
2. The apparatus according to claim 1, wherein the apparatus further comprises: the residual ammonia water treatment device also comprises a flash tank, the flash tank is connected with a water discharge pipe orifice of the ammonia still through a pipeline, and an exhaust port at the upper part of the flash tank is connected with an inlet of the ammonia still;
the liquid outlet of the flash tank is connected with the liquid inlet of the cyclone separator, and a second water pump is further arranged between the flash tank and the cyclone separator.
3. The apparatus for treating residual ammonia water in a coking process according to claim 2, wherein: and heat exchange and pressurization devices are also arranged on the exhaust port at the upper part of the flash tank and the air inlet pipeline of the ammonia still.
4. The apparatus according to claim 1, wherein the apparatus further comprises: and a cooling water pipe is further wound on the peripheral wall of the settling tank, and the water outlet end of the cooling water pipe is connected with the inlet end of the steam generating device.
5. The apparatus for treating residual ammonia water in a coking process according to any one of claims 1 to 4, characterized in that: and a filter is also arranged between the settling tank and the first water pump.
6. The apparatus according to claim 1, wherein the apparatus further comprises: and the front end and the rear end of the tube pass of the heat exchanger are respectively provided with a temperature measuring device.
7. The apparatus for treating residual ammonia water in a coking process according to claim 6, wherein: and the front end of the tube pass of the heat exchanger is also provided with a flow regulating electromagnetic valve, and the temperature measuring device and the flow regulating electromagnetic valve are electrically connected with a controller.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202020360328.5U CN211972044U (en) | 2020-03-20 | 2020-03-20 | Surplus aqueous ammonia processing apparatus in coking process |
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| CN202020360328.5U CN211972044U (en) | 2020-03-20 | 2020-03-20 | Surplus aqueous ammonia processing apparatus in coking process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114853119A (en) * | 2022-06-21 | 2022-08-05 | 广东韶钢松山股份有限公司 | Ammonia still blowdown water treatment facilities and coal gas clean system |
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2020
- 2020-03-20 CN CN202020360328.5U patent/CN211972044U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114853119A (en) * | 2022-06-21 | 2022-08-05 | 广东韶钢松山股份有限公司 | Ammonia still blowdown water treatment facilities and coal gas clean system |
| CN114853119B (en) * | 2022-06-21 | 2023-08-04 | 广东韶钢松山股份有限公司 | Ammonia still sewage treatment device and gas purification system |
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