CN205710629U - A kind of coke oven gas purification system and condensed fluid processing subsystem thereof - Google Patents
A kind of coke oven gas purification system and condensed fluid processing subsystem thereof Download PDFInfo
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- CN205710629U CN205710629U CN201620622490.3U CN201620622490U CN205710629U CN 205710629 U CN205710629 U CN 205710629U CN 201620622490 U CN201620622490 U CN 201620622490U CN 205710629 U CN205710629 U CN 205710629U
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Abstract
The utility model discloses the condensed fluid processing subsystem of a kind of coke oven gas purification system, including in mechanical settling tank, tar slag chute, mixing liquid bath, residual oil pump, mixture pump, de oiling hydrocyclone, water, de oiling hydrocyclone, ammonia medial launder, oil remove water cyclone and tar medial launder；The condensed fluid produced during gas purification utilizes eddy flow centrifugal sedimentation principle to achieve the separation of slag, oil, water, it is achieved that the instant process of condensed fluid, disengaging time is short, and separating effect is more preferable, decreases equipment, invests low, takes up an area little.This utility model additionally provides a kind of coke oven gas purification system including above-mentioned condensed fluid processing subsystem.
Description
Technical field
This utility model relates to coking gas purification technical field, especially relate to a kind of coke oven gas purification system and
Condensed fluid processing subsystem.
Background technology
The raw coke oven gas produced in process of coking enters gas-liquid separator after cyclic ammonia water sprinkling is cooled to 82～86 DEG C,
After gas-liquid separation, coal gas enters primary cooler, is cooled with circulating water to about 22 DEG C, and the coal gas after cooling traps tar through electric fishing
After mist successively through aerator, desulfurization, sulfur ammonium, eventually the coldest, wash benzene operation, obtain industrial purified gas.
In gas purification processing procedure, all produce condensation at gas-liquid separator, primary cooler, electrical tar precipitator and whole cooler
Liquid.At present, condensed fluid carries out the separation of condensed fluid generally by mechanical settling tank or tar ammonia water separator, obtains tar
Slag, tar and ammonia.This technique is the separation that the method utilizing quiescent settling to separate carries out each component, and quiescent time is long, point
From weak effect, equipment is huge, takes up an area big, investment height.
Therefore, how to provide that a kind of disengaging time is shorter, the preferable condensate water processing system of separating effect is current ability
Field technique personnel need badly and solve the technical problem that.
Utility model content
In view of this, the purpose of this utility model is to provide the condensed fluid process subsystem of a kind of coke oven gas purification system
System, this condensed water processing subsystem is capable of the instant separation of condensed fluid, reduces the sedimentation time, improve separating effect, reduce
Equipment takes up an area, and reduces investment.Another one purpose of the present utility model is to provide one and includes above-mentioned condensed fluid processing subsystem
Coke oven gas purification system.
For solving above-mentioned technical problem, the technical scheme that this utility model provides is:
The condensed fluid processing subsystem of a kind of coke oven gas purification system, including mechanical settling tank, tar slag chute, mixing
In liquid bath, residual oil pump, mixture pump, de oiling hydrocyclone, water in de oiling hydrocyclone, ammonia medial launder, oil except water cyclone and
Tar medial launder；
Described mechanical settling tank includes the condensed fluid feed liquor for introducing produced condensed fluid in coke oven gas purification system
Mouthful, for discharge tar slag tar slag outlet, for discharging the ammonia water and tar oil mixture outlet of ammonia water and tar oil mixture；
The condensed fluid inlet of described mechanical settling tank connects with the condensed fluid liquid source in coke oven gas purification system, institute
The tar slag outlet stating mechanical settling tank connects with the entrance of described tar slag chute, the ammonia water and tar oil of described mechanical settling tank
Mixture outlet connects with the inlet of described mixing liquid bath；
The bottom of described mixing liquid bath is provided with the residual oil outlet for discharging mixtures of residua and for discharging mixed liquor
Mixture export, the outlet of described residual oil connects with the entrance of described residual oil pump, described mixture export and described mixture pump
Entrance connection, described mixed liquor delivery side of pump connects with the inlet of described de oiling hydrocyclone；
Described de oiling hydrocyclone include the rich water product obtained after discharging cyclonic separation rich water outlet with for arranging
The oil rich outlet of the rich oil product obtained after going out cyclonic separation, the rich water outlet of described de oiling hydrocyclone and oil removing rotation in described water
The inlet connection of stream device, the oil rich outlet of described de oiling hydrocyclone connects with the inlet removing water cyclone in described oil；
In described water, de oiling hydrocyclone includes the rich water outlet of the rich water product obtained after discharging cyclonic separation and uses
The oil rich outlet of the rich oil product obtained after discharging cyclonic separation, in described water, the rich water of de oiling hydrocyclone exports and described ammonia
The inlet connection of water medial launder, inlet except water cyclone in the oil rich outlet of de oiling hydrocyclone and described oil in described water
Connection；
Except water cyclone includes the rich water outlet of the rich water product obtained after discharging cyclonic separation and uses in described oil
The oil rich outlet of the rich oil product obtained after discharging cyclonic separation, except oil rich outlet and described Jiao of water cyclone in described oil
The inlet connection of oil medial launder, except rich water outlet and the inlet of de oiling hydrocyclone in described water of water cyclone in described oil
Connection.
This utility model also provides for a kind of coke oven gas purification system, including gas-liquid separator, primary cooler, electrically trapped tar oil
Device, aerator, desulfurizing tower, saturator, whole cooler, wash benzene column, wash naphthalene tower and condensed water processing subsystem, at described condensed water
Reason subsystem is above-mentioned condensed water processing subsystem.
Preferably, the condensate outlet of described gas-liquid separator connects with the inlet of condensation liquid bath, described condensation liquid bath
Liquid outlet connected with the condensed fluid inlet of described mechanical settling tank by condensate pump.
Preferably, the condensate outlet of described primary cooler connects with the inlet of condensation liquid bath, going out of described condensation liquid bath
Liquid mouth is connected with the condensed fluid inlet of described mechanical settling tank by condensate pump.
Preferably, the condensate outlet of described electrical tar precipitator connects with the inlet of condensation liquid bath, described condensation liquid bath
Liquid outlet connected with the condensed fluid inlet of described mechanical settling tank by condensate pump.
Preferably, the condensate outlet of described aerator connects with the inlet of condensation liquid bath, going out of described condensation liquid bath
Liquid mouth is connected with the condensed fluid inlet of described mechanical settling tank by condensate pump.
Preferably, the condensate outlet of described whole cooler connects with the inlet of condensation liquid bath, going out of described condensation liquid bath
Liquid mouth is connected with the condensed fluid inlet of described mechanical settling tank by condensate pump.
Compared with prior art, the beneficial effects of the utility model are:
1, the condensed fluid produced during gas purification utilizes eddy flow centrifugal sedimentation principle to achieve the separation of slag, oil, water,
Achieving the instant process of condensed fluid, disengaging time is short, and separating effect is more preferable, decreases equipment, invests low, takes up an area little.
2, use eddy flow centrifugal sedimentation principle separation condensed fluid, improve oil-water separation, reduce in ammonia oil and
The content of float, decreases or has stopped the blocking of coke oven ammonia insufflation showerhead, simplifies the process technique of ammonia simultaneously, contracting
Short technological process, reduces investment, improves ammonia still process operation.
3, utilize cyclone separation process to carry out dehydration of tar, advantageously reduce tar water, optimize dehydrating operations, have
It is beneficial to reduce dewatered steam consumption.
4, using eddy flow centrifugal sedimentation principle separation condensed fluid, power consumption is low.
5, in this utility model, de oiling hydrocyclone, water remove water cyclone, segregation apparatus in de oiling hydrocyclone and oil
Little, flexible arrangement, floor space is little.
6, residue (circulation) ammonia cyclone deoiling technical operation are reliable and stable, and automaticity is high, convenient operating maintenance.
Accompanying drawing explanation
The operation principle schematic diagram of the coke oven gas purification system that Fig. 1 provides for this utility model embodiment.
In figure, 1 gas-liquid separator, 2 primary coolers, 3 electrical tar precipitators, 4 aerators, 5 desulfurizing towers, 6 saturators, 7 whole coolers,
8 wash benzene column, and 9 wash naphthalene tower, 10 mechanical settling tanks, 11 mixing liquid baths, and 12 mixture pumps, 13 de oiling hydrocyclones, except water in 14 oil
Cyclone, 15 tar medial launders, de oiling hydrocyclone in 16 water, 17 ammonia medial launders, 18 residual oil pumps, 19 tar slag chutes.
Detailed description of the invention
For making the purpose of this utility model embodiment, technical scheme and advantage clearer, new below in conjunction with this practicality
Accompanying drawing in type embodiment, is clearly and completely described the technical scheme in this utility model embodiment, it is clear that retouched
The embodiment stated is a part of embodiment of the present utility model rather than whole embodiments.Based on the reality in this utility model
Execute example, the every other embodiment that those of ordinary skill in the art are obtained on the premise of not making creative work, all
Belong to the scope of this utility model protection.
As it is shown in figure 1, the operation principle signal of the coke oven gas purification system that provides for this utility model embodiment of Fig. 1
Figure.
This utility model provides the condensed fluid processing subsystem of a kind of coke oven gas purification system, clarifies including mechanization
Groove 10, tar slag chute 19, mixing liquid bath 11, residual oil pump 18, mixture pump 12, de oiling hydrocyclone 13, water in de oiling hydrocyclone 16,
Except water cyclone 14 and tar medial launder 15 in ammonia medial launder 17, oil；
Described mechanical settling tank 10 includes entering for introducing the condensed fluid of produced condensed fluid in coke oven gas purification system
Liquid mouth, for discharge tar slag tar slag outlet, for discharging the ammonia water and tar oil mixture outlet of ammonia water and tar oil mixture；
The condensed fluid inlet of described mechanical settling tank 10 connects with the condensed fluid liquid source in coke oven gas purification system,
The tar slag outlet of described mechanical settling tank 10 connects with the entrance of described tar slag chute 19, described mechanical settling tank 10
Ammonia water and tar oil mixture outlet connects with the inlet of described mixing liquid bath 11；
The residual oil outlet that the bottom of described mixing liquid bath 11 is provided with for discharging mixtures of residua mixes with for discharging
The mixture export of liquid, the outlet of described residual oil connects with the entrance of described residual oil pump 18, and described mixture export mixes with described
The entrance connection of liquid pump 12, the outlet of described mixture pump 12 connects with the inlet of described de oiling hydrocyclone 13；
The rich water outlet of the rich water product that described de oiling hydrocyclone 13 includes obtaining after discharging cyclonic separation with for
The oil rich outlet of the rich oil product obtained after discharging cyclonic separation, the rich water outlet of described de oiling hydrocyclone 13 removes in described water
The inlet connection of oil cyclone 16, except the feed liquor of water cyclone 14 in the oil rich outlet of described de oiling hydrocyclone 13 and described oil
Mouth connection；
In described water the rich water outlet of the rich water product that de oiling hydrocyclone 16 includes obtaining after discharging cyclonic separation with
The oil rich outlet of the rich oil product obtained after discharging cyclonic separation, in described water, the rich water of de oiling hydrocyclone 16 exports and institute
State the inlet connection of ammonia medial launder 17, described water removes water cyclone in the oil rich outlet of de oiling hydrocyclone 16 and described oil
The inlet connection of 14；
The rich water outlet of the rich water product including obtaining after discharging cyclonic separation except water cyclone 14 in described oil with
The oil rich outlet of the rich oil product obtained after discharging cyclonic separation, except oil rich outlet and the institute of water cyclone 14 in described oil
State the inlet connection of tar medial launder 15, except rich water outlet and the de oiling hydrocyclone in described water of water cyclone 14 in described oil
The inlet connection of 16.
This utility model additionally provides a kind of coke oven gas purification system, including gas-liquid separator 1, primary cooler 2, electric tar
Oil device 3, aerator 4, desulfurizing tower 5, saturator 6, whole cooler 7, wash benzene column 8, wash naphthalene tower 9 and condensed water processing subsystem, institute
Stating condensed water processing subsystem is above-mentioned condensed water processing subsystem.
In an embodiment of the present utility model, the condensate outlet of described gas-liquid separator 1 enters with condensation liquid bath
Liquid mouth connects, and the liquid outlet of described condensation liquid bath is connected by the condensed fluid inlet of condensate pump with described mechanical settling tank 10
Logical.
In an embodiment of the present utility model, the condensate outlet of described primary cooler 2 and the inlet condensing liquid bath
Connection, the liquid outlet of described condensation liquid bath is connected with the condensed fluid inlet of described mechanical settling tank 10 by condensate pump.
In an embodiment of the present utility model, the condensate outlet of described electrical tar precipitator 3 enters with condensation liquid bath
Liquid mouth connects, and the liquid outlet of described condensation liquid bath is connected by the condensed fluid inlet of condensate pump with described mechanical settling tank 10
Logical.
In an embodiment of the present utility model, the condensate outlet of described aerator 4 and the inlet condensing liquid bath
Connection, the liquid outlet of described condensation liquid bath is connected with the condensed fluid inlet of described mechanical settling tank 10 by condensate pump.
In an embodiment of the present utility model, the condensate outlet of described whole cooler 7 and the inlet condensing liquid bath
Connection, the liquid outlet of described condensation liquid bath is connected with the condensed fluid inlet of described mechanical settling tank 10 by condensate pump.
As it is shown in figure 1, the raw coke oven gas from coke oven sequentially enters gas-liquid separator 1, primary cooler 2, electrical tar precipitator 3, drum
Blower fan 4, desulfurizing tower 5, saturator 6, whole cooler 7, wash benzene column 8 and wash naphthalene tower 9 after to coal gas user, complete gas purification process.
During gas purification, the isolated condensed fluid of gas-liquid separator 1 is from flowing into mechanical settling tank 10；Primary cooler
2 condensed fluid produced import condensation liquid bath, and mechanical settling tank 10 delivered to by condensed liquid pump；Electrical tar precipitator 3 is isolated cold
Lime set enters condensation liquid bath, and mechanical settling tank 10 delivered to by condensed liquid pump；The condensed fluid that aerator 4 produces enters condensed fluid
Groove, condensed liquid pump is delivered to mechanical settling tank 10；The whole isolated condensed fluid of cooler 7 enters condensation liquid bath, condensed liquid
Transport pump is to mechanical settling tank 10.
First the condensed fluid produced during gas purification comes together in mechanical settling tank 10, carries out ammonia water and tar oil mixture
With the separation of tar slag, tar slag is separated, and puts into tar slag chute and stores, and periodically delivers to return for coal join in coking coal；Remove
Ammonia water and tar oil mixture after slag is from flowing into mixed liquor groove 11.
Described mixing liquid bath 11 is cone bottom structure, and bottom has residual oil outlet to connect the entrance of residual oil pump 18, and residual oil pump 18 goes out
Mouth connection mechanical settling tank 10, delivers to machine by coke powder, tar and the float of mixing liquid bath 11 bottom sediments by residual oil pump 18
Tool defecator 10, separates tar slag further.It is additionally provided with mixture export bottom mixing liquid bath 11, connects mixture pump 12
Entrance.
In mixing liquid bath 11, the blended liquid pump of mixed liquor 12 is extracted out, delivers to the inlet of de oiling hydrocyclone 13, utilizes eddy flow
Centrifugal sedimentation principle realizes the initial gross separation of ammonia and tar.
The rich water outlet of described de oiling hydrocyclone 13 connects with the inlet of de oiling hydrocyclone 16 in described water, described oil removing
The oil rich outlet of cyclone 13 connects with the inlet removing water cyclone 14 in described oil, carries out the further oil removing of ammonia respectively
Further dehydration with tar.
Isolate tar through de oiling hydrocyclone 13 to be sent directly in oil except water cyclone 14, utilize eddy flow centrifugal sedimentation principle
Isolation technics carries out the dehydrating operations of tar.
The oil rich outlet removing water cyclone 14 in oil connects the entrance of tar medial launder 15, and tar is sent directly in the middle of tar
Groove 15.Oil connects the inlet of de oiling hydrocyclone 16 in water except the rich water outlet of water cyclone 14, isolated ammonia with remove
The oil isolated ammonia of cyclone 13 enters de oiling hydrocyclone 16 in water, further oil removing jointly, reduces ammonia oil-containing.
Isolate ammonia through de oiling hydrocyclone 13 and be sent directly into de oiling hydrocyclone 16 in water, utilize eddy flow centrifugal sedimentation to separate
Principle carries out the further removing oil of ammonia, reduces ammonia oil-containing.In water, the rich water outlet of de oiling hydrocyclone 16 connects in the middle of ammonia
The inlet of groove 17, i.e. ammonia are from flowing into ammonia medial launder 17.Except water during in water, the oil rich outlet of de oiling hydrocyclone 16 connects oil
The inlet of cyclone 14, in water, the isolated tar of de oiling hydrocyclone 16 tar isolated with de oiling hydrocyclone 13 mixes
Enter in oil except water cyclone 14, be further dehydrated, reduce tar aqueous.
This utility model is to utilize cyclonic separation principle to separate the condensed fluid formed in coke-stove gas purification process,
Replacing the static separation of current sector application by cyclonic separation, be conducive to improving separating effect, reduction tar is aqueous and ammonia contains
Oil, beneficially coking technique, simplify ammonia oil removing flow process, reduction equipment, invest and take up an area.This patent is by coke oven gas purification mistake
Cheng Zhong, at the condensed fluid that gas-liquid separator, primary cooler, electrical tar precipitator, aerator, whole cooler produce, first passes through mechanization
Defecator 10 removes tar slag, then utilizes de oiling hydrocyclone 13 to realize at the beginning of tar and ammonia in the ammonia water and tar oil mixture of slagging-off
Step separates, and followed by utilizes cyclone separation process to operate the ammonia oil removing after initial gross separation and dehydration of tar, finally obtains Jiao
Oil and ammonia.This utility model utilizes and cyclone separation process is applied to the separation of condensed fluid during coke oven gas purification, carries
High separation efficiency, reduces equipment, reduces investment, reduces that tar is aqueous and ammonia oil-containing, for coke oven, ammonia still process etc. simultaneously
Operation creates favourable conditions.
In this utility model, eddy flow centrifugal sedimentation isolation technics and realize the cyclone of this isolation technics and be existing skill
Art, those skilled in the art are easily achieved, and are not described in detail at this.
The explanation of above example is only intended to help to understand method of the present utility model and core concept thereof.Should refer to
Go out, for those skilled in the art, on the premise of without departing from this utility model principle, it is also possible to this
Utility model carries out some improvement and modification, and these improve and modification also falls into this utility model scope of the claims
In.
Described above to the disclosed embodiments, makes professional and technical personnel in the field be capable of or uses this practicality new
Type.Multiple amendment for these embodiments is apparent from for those skilled in the art, defined herein
General Principle can realize in other embodiments in the case of without departing from spirit or scope of the present utility model.Therefore,
This utility model is not intended to be limited to the embodiments shown herein, and is to fit to and principles disclosed herein and new
The widest range that grain husk feature is consistent.
Claims (7)
1. the condensed fluid processing subsystem of a coke oven gas purification system, it is characterised in that include mechanical settling tank, tar
Slag chute, mixing liquid bath, residual oil pump, mixture pump, de oiling hydrocyclone, water revolve except water in de oiling hydrocyclone, ammonia medial launder, oil
Stream device and tar medial launder；
Described mechanical settling tank includes for introducing the condensed fluid inlet of produced condensed fluid in coke oven gas purification system, use
In discharging the tar slag outlet of tar slag, for discharging the ammonia water and tar oil mixture outlet of ammonia water and tar oil mixture；
The condensed fluid inlet of described mechanical settling tank connects with the condensed fluid liquid source in coke oven gas purification system, described machine
The tar slag outlet of tool defecator connects with the entrance of described tar slag chute, the ammonia water and tar oil mixing of described mechanical settling tank
Thing outlet connects with the inlet of described mixing liquid bath；
The bottom of described mixing liquid bath is provided with the residual oil outlet for discharging mixtures of residua and for discharging the mixed of mixed liquor
Conjunction liquid exports, and the outlet of described residual oil connects with the entrance of described residual oil pump, and described mixture export enters with described mixture pump
Mouth connection, described mixed liquor delivery side of pump connects with the inlet of described de oiling hydrocyclone；
Described de oiling hydrocyclone includes the rich water outlet of the rich water product obtained after discharging cyclonic separation and for discharging rotation
The oil rich outlet of the rich oil product obtained after flow separation, rich water outlet and the de oiling hydrocyclone in described water of described de oiling hydrocyclone
Inlet connection, the oil rich outlet of described de oiling hydrocyclone with in described oil remove water cyclone inlet connect；
In described water de oiling hydrocyclone include the rich water product obtained after discharging cyclonic separation rich water outlet with for arranging
The oil rich outlet of the rich oil product obtained after going out cyclonic separation, in described water, the rich water of de oiling hydrocyclone exports and in described ammonia
Between the inlet connection of groove, in described water in the oil rich outlet of de oiling hydrocyclone and described oil except water cyclone inlet even
Logical；
In described oil except water cyclone include the rich water product obtained after discharging cyclonic separation rich water outlet with for arranging
The oil rich outlet of the rich oil product obtained after going out cyclonic separation, removes in described oil in oil rich outlet and the described tar of water cyclone
Between the inlet connection of groove, in described oil except water cyclone rich water outlet with the inlet of de oiling hydrocyclone in described water even
Logical.
2. a coke oven gas purification system, including gas-liquid separator, primary cooler, electrical tar precipitator, aerator, desulfurizing tower, satisfies
With device, whole cooler, wash benzene column, wash naphthalene tower and condensed water processing subsystem, it is characterised in that described condensed water processing subsystem
For the condensed water processing subsystem described in claim 1.
Coke oven gas purification system the most according to claim 2, it is characterised in that the condensed fluid of described gas-liquid separator goes out
Mouth connects with the inlet of condensation liquid bath, and the liquid outlet of described condensation liquid bath is by condensate pump and described mechanical settling tank
Condensed fluid inlet connects.
Coke oven gas purification system the most according to claim 2, it is characterised in that the condensate outlet of described primary cooler with
The inlet connection of condensation liquid bath, the liquid outlet of described condensation liquid bath is by the condensation of condensate pump with described mechanical settling tank
Liquid inlet connects.
Coke oven gas purification system the most according to claim 2, it is characterised in that the condensed fluid of described electrical tar precipitator goes out
Mouth connects with the inlet of condensation liquid bath, and the liquid outlet of described condensation liquid bath is by condensate pump and described mechanical settling tank
Condensed fluid inlet connects.
Coke oven gas purification system the most according to claim 2, it is characterised in that the condensate outlet of described aerator with
The inlet connection of condensation liquid bath, the liquid outlet of described condensation liquid bath is by the condensation of condensate pump with described mechanical settling tank
Liquid inlet connects.
Coke oven gas purification system the most according to claim 2, it is characterised in that the condensate outlet of described whole cooler with
The inlet connection of condensation liquid bath, the liquid outlet of described condensation liquid bath is by the condensation of condensate pump with described mechanical settling tank
Liquid inlet connects.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201620622490.3U CN205710629U (en) | 2016-06-22 | 2016-06-22 | A kind of coke oven gas purification system and condensed fluid processing subsystem thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201620622490.3U CN205710629U (en) | 2016-06-22 | 2016-06-22 | A kind of coke oven gas purification system and condensed fluid processing subsystem thereof |
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| Publication Number | Publication Date |
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| CN205710629U true CN205710629U (en) | 2016-11-23 |
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| CN201620622490.3U Expired - Fee Related CN205710629U (en) | 2016-06-22 | 2016-06-22 | A kind of coke oven gas purification system and condensed fluid processing subsystem thereof |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106010670A (en) * | 2016-06-22 | 2016-10-12 | 山东钢铁股份有限公司 | Coke oven gas purification system and condensate treatment subsystem thereof |
-
2016
- 2016-06-22 CN CN201620622490.3U patent/CN205710629U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106010670A (en) * | 2016-06-22 | 2016-10-12 | 山东钢铁股份有限公司 | Coke oven gas purification system and condensate treatment subsystem thereof |
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| C14 | Grant of patent or utility model | ||
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20161123 Termination date: 20190622 |