CN104962322B - Coke oven gas purification system - Google Patents
Coke oven gas purification system Download PDFInfo
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- CN104962322B CN104962322B CN201510321301.9A CN201510321301A CN104962322B CN 104962322 B CN104962322 B CN 104962322B CN 201510321301 A CN201510321301 A CN 201510321301A CN 104962322 B CN104962322 B CN 104962322B
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Abstract
The invention discloses coke oven gas purification system, including：Saturator, soft water storage tank, final cooling tower, crude benzol separated water storage tank, ammonia steaming device and sewage-treatment plant, soft water storage tank connects saturator, saturator is connected with the hypomere air inlet of final cooling tower, the hypomere water outlet of final cooling tower is connected with the first delivery pump, first delivery pump is connected with First Heat Exchanger, First Heat Exchanger is connected with the hypomere water inlet of final cooling tower, the epimere water outlet of final cooling tower is connected with the second delivery pump, second delivery pump is connected with the second heat exchanger, and the second heat exchanger is connected with the epimere water inlet of final cooling tower；4th pipeline even steam ammonia device, ammonia steaming device connects sewage-treatment plant, crude benzol separated water storage tank is connected by the 11st pipeline equipped with submerged pump and the 3rd valve with the 6th pipeline, and the 4th pipeline is also connected by the 12nd pipeline equipped with the 4th valve with moisturizing manifold.The present invention has the advantages that enterprise's production and application cost is low.
Description
Technical field
The present invention relates to the coke oven gas purification system of the waste water recycling such as coke-oven plant's end cold water and crude benzol process separated water
System.
Background technology
Coke oven gas purification system at present（As shown in Figure 1）Including：Saturator 40, soft water storage tank 41, final cooling tower 42, crude benzol
Separated water storage tank 43, ammonia steaming device 44 and sewage-treatment plant 45, soft water storage tank 41 is by being provided with the first valve 46
First pipeline 47 is connected with the water supplement port of saturator 40, and the gas outlet of saturator 40 passes through the second pipeline 48 and final cooling tower 42
Hypomere air inlet is connected, and the hypomere water outlet of final cooling tower 42 is connected by the 3rd pipeline 49 with the water inlet of the first delivery pump 50
Logical, the water outlet of the first delivery pump 50 is connected by the 4th pipeline 51 with the import of First Heat Exchanger 52, First Heat Exchanger 52
Outlet be connected by the 5th pipeline 53 with the hypomere water inlet of final cooling tower 42, the epimere water outlet of final cooling tower 42 passes through the 6th
Pipeline 54 is connected with the water inlet of the second delivery pump 55, and the water outlet of the second delivery pump 55 is changed by the 7th pipeline 56 with second
The import of hot device 57 is connected, and the outlet of the second heat exchanger 57 is connected by the 8th pipeline 58 with the epimere water inlet of final cooling tower 42
Logical, the water outlet of first delivery pump 50 also connects ammonia steaming device 44 by being provided with the 9th pipeline 60 of the second valve 59,
The crude benzol separated water storage tank 43 connects ammonia steaming device 44 by the tenth pipeline 62 of submerged pump 61, and ammonia steaming device 44 leads to again
Cross the 11st pipeline 63 connection sewage-treatment plant 45.The coke oven gas purification operation principle of above-mentioned coke gas cleaning system is：
The air inlet of dry gas from saturator 40 is passed through saturator 40, and the inside of saturator 40 can spray dilute sulfuric acid downwards, and dilute sulfuric acid is with doing
Coal gas can be with the ammonia reaction generation ammonium sulfate in dry gas when contacting, so as to remove the ammonia in dry gas, dry gas is through full
Become wet gas after removing ammonia with device and be discharged into the second pipeline 48 from the gas outlet of saturator 40, then enter final cooling tower through the second pipeline 48
42 hypomere, during wet gas moves in final cooling tower 42 from hypomere to epimere, the end of the hypomere bottom of final cooling tower 42 is cold
Water can enter the 4th pipeline 51 through the 3rd pipeline 49 successively under the action of the first delivery pump 50, and the end into the 4th pipeline 51 is cold
Water is partly into First Heat Exchanger 52 and is cooled down, the end cold water hypomere through the 5th pipeline 53 from final cooling tower 42 again after cooling
Water inlet reenters 42 hypomere of final cooling tower, and one of spraying cooling is carried out to the wet gas that moves up so as to circulate, into the
Another part end cold water of four pipelines 51 then enters ammonia steaming device 44 through the 9th pipeline 60, then from ammonia steaming device 44 through the 11st pipe
Road 63 enters sewage-treatment plant 45 and carries out sewage disposal；And the wet gas after one of spraying cooling may proceed to be moved upward to
The epimere of final cooling tower 42, wet gas is during the epimere of final cooling tower 42 is moved to top gas outlet, the epimere of final cooling tower 42
Whole cold water under the action of the second delivery pump 55 can successively through the 6th pipeline 54, the 7th pipeline 56 enter the second heat exchanger 57 into
Row cooling, end cold water after cooling reenter final cooling tower epimere through the 8th pipeline 58 from the epimere water inlet of final cooling tower 42 again,
Two spraying coolings are carried out to the wet gas moved down, wet gas forms saturation coal gas from final cooling tower after two spraying coolings
Top gas outlet discharge；It is thick in crude benzol separated water storage tank 43 while final cooling tower 42 carries out cold eventually to wet gas
Benzene distillation separates water can also enter ammonia steaming device 44 under the action of submerged pump 61 through the tenth pipeline 62, then be passed through from ammonia steaming device 44
11st pipeline 63 enters sewage-treatment plant 45 and carries out sewage disposal；
The shortcomings that above-mentioned coke oven gas purification system is：（1）Since the operation principle of saturator is with doing by dilute sulfuric acid
Ammonia reaction in coal gas produces sulfate of ammoniac to remove the ammonia in dry gas, female when the ammonium sulfate concentrations in saturator are supersaturated
Just have substantial amounts of ammonium sulfate crystallization particle in liquid to produce, while part of sulfuric acid crystalline ammonium can be attached to the inner wall of saturator, make
Coal gas flow area in saturator reduces, and increases gas resistance, when gas resistance increases to more than 2000Pa, it will give
Whole coke oven gas purification system brings security risk, so when the gas resistance of saturator is more than 2000Pa, it is necessary to satisfying
Mother liquor is diluted with soft water is added in device, ammonium sulfate liquor is changed into undersaturated condition from hypersaturated state, makes to be attached to saturation
Ammonium sulfate crystallization on device inner wall is dissolved in undersaturated mother liquor, achievees the purpose that to reduce gas resistance in saturator；So
To ensure that the gas resistance in saturator meets normal production requirement, it is necessary to periodically to mending soft water in saturator, cause soft water
Usage amount is big, and not only enterprise's production and application is of high cost, but also the waste water produced is also more, at the waste water for making terminal sewage-treatment plant
Reason amount is big, increases cost of sewage disposal；（2）Since crude benzol distillation process produces and is stored in crude benzol separated water storage tank
Crude benzol separated water and the unnecessary whole cold water that produces of final cooling tower also all directly enter sewage-treatment plant through ammonia steaming device, into
One step increases the wastewater treatment capacity of terminal sewage-treatment plant, further increases cost of sewage disposal, further increases
Enterprise's production and application cost.
The content of the invention
The object of the present invention is to provide a kind of low coke oven gas purification system of enterprise's production and application cost.
To achieve the above object, present invention employs following technical solution：The coke oven gas purification system, including：
Saturator, soft water storage tank, final cooling tower, crude benzol separated water storage tank, ammonia steaming device and sewage-treatment plant, soft water storage tank pass through
The first pipeline equipped with the first valve is connected with connecting the moisturizing manifold of saturator water supplement port, and the gas outlet of saturator passes through the
Two pipelines are connected with the hypomere air inlet of final cooling tower, and the hypomere water outlet of final cooling tower passes through the 3rd pipeline and the first delivery pump
Water inlet is connected, and the water outlet of the first delivery pump is connected by the 4th pipeline with the import of First Heat Exchanger, the first heat exchange
The outlet of device is connected by the 5th pipeline with the hypomere water inlet of final cooling tower, and the epimere water outlet of final cooling tower passes through the 6th pipeline
It is connected with the water inlet of the second delivery pump, the import phase that the water outlet of the second delivery pump passes through the 7th pipeline and the second heat exchanger
Connection, the outlet of the second heat exchanger is connected by the 8th pipeline with the epimere water inlet of final cooling tower；4th pipeline passes through
The 9th pipeline connection ammonia steaming device equipped with the second valve, ammonia steaming device are connected by the tenth pipeline with sewage-treatment plant,
Crude benzol separated water storage tank is connected by the 11st pipeline equipped with submerged pump and the 3rd valve with the 6th pipeline, and described
Four pipelines are also connected by the 12nd pipeline equipped with the 4th valve with moisturizing manifold.
Further, foregoing coke oven gas purification system, wherein：Increase-volume dashpot is provided with final cooling tower side, is increased
The bottom for holding dashpot is connected by the 13rd pipeline equipped with the 5th valve with the bottom of final cooling tower, the top of increase-volume dashpot
Portion is connected by the 14th pipeline equipped with the 6th valve with the top of final cooling tower hypomere.
Further, foregoing coke oven gas purification system, wherein：The 7th valve is installed on the 13rd pipeline.
Further, foregoing coke oven gas purification system, wherein：The 8th valve is installed on the 14th pipeline.
Further, foregoing coke oven gas purification system, wherein：The 9th valve is installed on the 11st pipeline.
Further, foregoing coke oven gas purification system, wherein：The tenth valve is installed on the 12nd pipeline.
The implementation of Pass through above-mentioned technical proposal, the beneficial effects of the invention are as follows：（1）Whole cold water part is cut be recycled to it is full
The soft water needed for saturator is replaced with device, so as to reduce the soft water magnitude of recruitment of saturator, and then effectively reduces sewage
The wastewater treatment capacity of processing unit, reduces enterprise's production and application cost；（2）Crude benzol distillation process is produced and is stored in crude benzol
Crude benzol separated water in separated water storage tank is delivered in final cooling tower, not only reduce further sewage-treatment plant
Wastewater treatment capacity, reduces enterprise production and application cost, and can effectively reduce in the whole cold water of final cooling tower it is various it is soluble from
The concentration of sub and insoluble impurity, it is ensured that the whole cold water of circulating and recovering to saturator meets the normal production of ammonium sulfate in saturator
It is required that.
Brief description of the drawings
Fig. 1 is the operation principle schematic diagram of the coke oven gas purification system shown in background technology.
Fig. 2 is the operation principle schematic diagram of coke oven gas purification system of the present invention.
Embodiment
The invention will be further described with specific embodiment below in conjunction with the accompanying drawings.
As shown in Fig. 2, the coke oven gas purification system, including：Saturator 1, soft water storage tank 2, final cooling tower 3, crude benzol
Separated water storage tank 4, ammonia steaming device 5 and sewage-treatment plant 6, soft water storage tank 2 pass through the first pipeline equipped with the first valve 7
8 are connected with connecting the moisturizing manifold 9 of 1 water supplement port of saturator, and the gas outlet of saturator passes through the second pipeline 10 and final cooling tower 3
Hypomere air inlet is connected, and the hypomere water outlet of final cooling tower 3 is connected by the 3rd pipeline 11 with the water inlet of the first delivery pump 12
Logical, the water outlet of the first delivery pump 12 is connected by the 4th pipeline 13 with the import of First Heat Exchanger 14, First Heat Exchanger 14
Outlet be connected by the 5th pipeline 15 with the hypomere water inlet of final cooling tower 3, the epimere water outlet of final cooling tower 3 passes through the 6th pipe
Road 16 is connected with the water inlet of the second delivery pump 17, and the water outlet of the second delivery pump 17 passes through the 7th pipeline 18 and the second heat exchange
The import of device 19 is connected, and the outlet of the second heat exchanger 19 is connected by the 8th pipeline 20 with the epimere water inlet of final cooling tower 3；
4th pipeline 13 connects ammonia steaming device 5 by the 9th pipeline 22 equipped with the second valve 21, and ammonia steaming device 5 passes through the tenth pipe
Road 23 is connected with sewage-treatment plant 6, and crude benzol separated water storage tank 4 passes through equipped with submerged pump 24 and the 3rd valve 25
11 pipelines 26 are connected with the 6th pipeline 16, and the 4th pipeline 13 also passes through the 12nd pipeline 28 equipped with the 4th valve 27
It is connected with moisturizing manifold 9；In the present embodiment, increase-volume dashpot 29, increase-volume dashpot 29 are provided with the side of final cooling tower 3
Bottom be connected by the 13rd pipeline 31 equipped with the 5th valve 30 with the bottom of final cooling tower 3, the top of increase-volume dashpot 29
Portion is connected by the 14th pipeline 33 equipped with the 6th valve 32 with the top of 3 hypomere of final cooling tower, passes through increase-volume dashpot 29
The moisture storage capacity of final cooling tower 3 can be effectively improved, the liquid level of final cooling tower hypomere can be prevented to be evacuated in 3 moisturizing of saturator, carried
The high operation stability of final cooling tower 3, and then improve the stability of whole waste water reuse system；In the present embodiment,
The 7th valve 34 is installed on 13 pipelines 31, so when the 5th valve 30 breaks down, can by the 7th valve 34 come
The 13rd pipeline 31 is controlled, further increases the stability of whole waste water reuse system；In the present embodiment, in the 14th pipe
8th valve 35 is installed on road 33, so when the 6th valve 32 breaks down, can be controlled by the 8th valve 35
14 pipelines 33, further increase the stability of whole waste water reuse system；In the present embodiment, on the 11st pipeline 26
9th valve 38 is installed, so when the 3rd valve 25 breaks down, control the tenth can be continued by the 9th valve 38
One pipeline, further increases the stability of whole waste water reuse system；In the present embodiment, installed on the 12nd pipeline 28
There is the tenth valve 39, so when the 4th valve 27 breaks down, control the 12nd can be continued by the 12nd pipeline 28
Pipeline, further increases the stability of whole waste water reuse system；
The operation principle of the present invention is as follows：
The first valve 7, the 4th valve 27, the 9th valve 38 are first closed, and opens remaining valve, then by dry gas from full
Saturator 1 is passed through with the air inlet of device 1, and the inside of saturator 1 can spray dilute sulfuric acid downwards, can be with when dilute sulfuric acid is contacted with dry gas
Ammonia reaction generation ammonium sulfate in dry gas, so as to remove the ammonia in dry gas, dry gas becomes after saturator removes ammonia
Wet gas is discharged into the second pipeline 10 from the gas outlet of saturator 1, then enters the hypomere of final cooling tower 3, wet gas through the second pipeline 10
During being moved in final cooling tower 3 from hypomere to epimere, the whole cold water of the hypomere bottom of final cooling tower 3 is in the first delivery pump 12
Enter the 4th pipeline 13 through the 3rd pipeline 11 under effect, the whole cold water into the 4th pipeline 13 is partly into First Heat Exchanger 14
Cooled down, end cold water after cooling is reentered under final cooling tower 3 through the 5th pipeline 15 from the hypomere water inlet of final cooling tower 3 again
Section, carries out one of spraying cooling, into another part end cold water of the 4th pipeline 13 so as to circulate to the wet gas moved up
Then enter ammonia steaming device 5 through the 9th pipeline 22, then dirt is carried out into sewage-treatment plant 6 from ammonia steaming device 5 through the tenth pipeline 23
Water process；And the wet gas after one of spraying cooling is continued to move up to the epimere of final cooling tower 3, wet gas is in final cooling tower 3
Epimere moved to top gas outlet during, the effect of the whole cold water of the epimere bottom of final cooling tower 3 in the second delivery pump 17
Under can be cooled down successively through the 6th pipeline 16, the 7th pipeline 18 into the second heat exchanger 19, end cold water after cooling is again through the
Eight pipelines 20 reenter final cooling tower epimere from the epimere water inlet of final cooling tower 3, and two sprays are carried out to the wet gas moved down
Leaching cooling, wet gas forms saturation coal gas after two spraying coolings and is discharged from the top gas outlet of final cooling tower, on final cooling tower 3
While the whole cold water of section is sent into final cooling tower by circulation, the crude benzol separated water in crude benzol separated water storage tank 4 can be in liquid
Through the 11st pipeline 26 also enter the 6th pipeline 16 under the action of lower pump 24, it is cold with end for being extracted out from the epimere bottom of final cooling tower 3
Water is sent into final cooling tower 3 by circulation together, and the crude benzol separated water in crude benzol separated water storage tank 4 can be reduced effectively end
The concentration of various soluble ions and insoluble impurity in the whole cold water of cold tower 3, it is ensured that the whole cold water quality in final cooling tower 3 meets
The normal production requirement of ammonium sulfate in saturator 1；During final cooling tower 3 is cold to wet medium gas progress end, the hypomere of final cooling tower 3
A part of whole cold water can be stored in by the 13rd pipeline 31 in increase-volume dashpot 29, increase-volume is delayed by the 14th pipeline 33
Jet-bedding 29 is vented, it is ensured that the liquid level for the whole cold water being stored in increase-volume dashpot 29 and the whole cold water of 3 hypomere of final cooling tower
Liquid level is consistent；
When water-refilling operation need to be carried out to saturator 1, the first valve 7, the 4th valve 27, the 9th valve 38 are opened, is made soft
Soft water in water storage tank 2 enters moisturizing manifold 9 through the first pipeline 8, while makes to be sent into the 4th pipeline 13 through the first delivery pump 12
Part end cold water in whole cold water also enters moisturizing manifold 9 through the 12nd pipeline, cold eventually into the soft water of moisturizing manifold 9 and part
Water supplement port of the water again through saturator 1 enters in saturator.
It is an advantage of the invention that：（1）Whole cold water part is cut and is recycled to saturator to replace the soft water needed for saturator,
So as to reduce the soft water magnitude of recruitment of saturator, and then the wastewater treatment capacity of sewage-treatment plant is effectively reduced, reduced
Enterprise's production and application cost；（2）Crude benzol distillation process is produced and is stored in the distillation of the crude benzol in crude benzol separated water storage tank
Separation water is delivered in final cooling tower, not only reduce further the wastewater treatment capacity of sewage-treatment plant, and reducing enterprise's production makes
With cost, and it can effectively reduce the concentration of various soluble ions and insoluble impurity in the whole cold water of final cooling tower, it is ensured that
The whole cold water of circulating and recovering to saturator meets the normal production requirement of ammonium sulfate in saturator.
Claims (5)
1. coke oven gas purification system, including：Saturator, soft water storage tank, final cooling tower, crude benzol separated water storage tank, ammonia still process dress
Put and sewage-treatment plant, soft water storage tank are total by moisturizing of the first pipeline equipped with the first valve with connecting saturator water supplement port
Pipe is connected, and the gas outlet of saturator is connected by the second pipeline with the hypomere air inlet of final cooling tower, and the hypomere of final cooling tower goes out
The mouth of a river is connected by the 3rd pipeline with the water inlet of the first delivery pump, and the water outlet of the first delivery pump passes through the 4th pipeline and
The import of one heat exchanger is connected, and the outlet of First Heat Exchanger is connected by the 5th pipeline with the hypomere water inlet of final cooling tower,
The epimere water outlet of final cooling tower is connected by the 6th pipeline with the water inlet of the second delivery pump, and the water outlet of the second delivery pump leads to
Cross the 7th pipeline with the import of the second heat exchanger to be connected, the outlet of the second heat exchanger passes through the 8th pipeline and the epimere of final cooling tower
Water inlet is connected；4th pipeline is passed through by the 9th pipeline connection ammonia steaming device equipped with the second valve, ammonia steaming device
Tenth pipeline is connected with sewage-treatment plant, it is characterised in that：Crude benzol separated water storage tank passes through equipped with submerged pump and
11st pipeline of three valves is connected with the 6th pipeline, and the 4th pipeline also passes through the 12nd pipeline equipped with the 4th valve
It is connected with moisturizing manifold, increase-volume dashpot is provided with final cooling tower side, the bottom of increase-volume dashpot passes through equipped with the 5th valve
13rd pipeline of door is connected with the bottom of final cooling tower, and the top of increase-volume dashpot passes through the 14th pipe equipped with the 6th valve
Road is connected with the top of final cooling tower hypomere.
2. coke oven gas purification system according to claim 1, it is characterised in that：The 7th is provided with the 13rd pipeline
Valve.
3. coke oven gas purification system according to claim 1, it is characterised in that：The 8th is provided with the 14th pipeline
Valve.
4. coke oven gas purification system according to claim 1, it is characterised in that：The 9th is provided with the 11st pipeline
Valve.
5. coke oven gas purification system according to claim 1, it is characterised in that：The tenth is provided with the 12nd pipeline
Valve.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510321301.9A CN104962322B (en) | 2015-06-12 | 2015-06-12 | Coke oven gas purification system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510321301.9A CN104962322B (en) | 2015-06-12 | 2015-06-12 | Coke oven gas purification system |
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| CN104962322A CN104962322A (en) | 2015-10-07 |
| CN104962322B true CN104962322B (en) | 2018-05-15 |
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| CN108661114A (en) * | 2018-05-17 | 2018-10-16 | 马鞍山钢铁股份有限公司 | A kind of automatic water-replenishing device and its control method of gas cleaning system |
| CN112707456A (en) * | 2020-12-21 | 2021-04-27 | 河南中子星节能科技有限公司 | Ammonia distillation system and ammonia distillation method |
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| CN101760251B (en) * | 2009-12-29 | 2013-05-29 | 中冶焦耐(大连)工程技术有限公司 | New water-saving, energy-saving and less-equipment corrosion process and device for purifying coke oven gas |
| CN102260541B (en) * | 2011-06-27 | 2013-11-06 | 马鞍山钢铁股份有限公司 | Naphthalene washing process in coke oven gas purification |
| DE102012107336A1 (en) * | 2012-08-09 | 2014-02-13 | Thyssenkrupp Uhde Gmbh | Process for the removal of aromatic hydrocarbons from Kokereigas with biodiesel as a washing liquid and apparatus for carrying out the method |
| CN204824767U (en) * | 2015-06-12 | 2015-12-02 | 江苏永钢集团有限公司 | Coke oven gas clean system |
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