CN105776695B - A kind of coking plant sour water abatement and the method for reuse - Google Patents
A kind of coking plant sour water abatement and the method for reuse Download PDFInfo
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- CN105776695B CN105776695B CN201610101442.4A CN201610101442A CN105776695B CN 105776695 B CN105776695 B CN 105776695B CN 201610101442 A CN201610101442 A CN 201610101442A CN 105776695 B CN105776695 B CN 105776695B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Abstract
The present invention provides a kind of reduction of coking plant sour water and reuse methods, to coking plant water, it drains link and carries out system optimization, reduce steam and water resources consumption, sour water tandem uses, sour water yield is reduced from source, reduce the sour water amount into subsequent acidic water stripper plant, multipath reuse strips after-purification water and reduces the sewage quantity for entering sewage farm end-o f-pipe -control device, mitigate acidic water stripping device, end sewage farm pressure, realize essential clean manufacturing and source water-saving and emission-reducing, it can realize the two-win of economic benefit and environmental benefit.
Description
Technical field
The present invention relates to technical field of petrochemical industry more particularly to a kind of coking plant sour water abatement and reuse sides
Method.
Background technology
In Sulfur-Containing Crude, the devices such as Atmospheric vacuum, catalytic cracking, delayed coking, hydrofinishing will be discharged for refinery
A large amount of sour waters (acid water) also contain phenol, cyanide and oil in sour water in addition to containing a large amount of hydrogen sulfide, ammonia nitrogen
Pollutant has strong stench, has corrosivity to equipment.Sour water generates and discharge, both to pretreatment link acid
Property water stripper plant have an impact, and to end sewage farm operation have restrictive function.With high-sulfurized, the peracid of processing crude oil
The increasingly strict and oil product of change degree getting worse, environment protectment protection cleans the increasingly raising of requirement, and oil refining enterprise contains
The generation of sulphur sewage, treating capacity will be on the increase, and cost of sewage disposal is also continuously increased.How sour water production is effectively optimized
Raw, processing and reuse mitigate the pressure of acid water pre-treatment means and end sewage farm, save processing cost, improve warp
Benefit of helping and environmental benefit, are each oil refining enterprise's questions of common concern.
Delayed coking unit water, draining link are more, are typical sour water generation device and sour water reuse
The big exemplary device of potentiality, carries out the management of coking plant sour water and optimization uses, and both has weight to the water-saving and emission-reducing of the present apparatus
It acts on, also has important reference and reference value to other devices.In recent years, many enterprises were reduced around coking plant
Sour water yield and raising sour water and stripping purified water reuse ratio have carried out work, but these work are mostly
Around some point or certain several local expansion, system is not carried out to device water, draining link, comprehensively, is integrally divided
Analysis and optimization, so causing the current sour water yield of device still larger, reuse amount is insufficient, and water-saving and emission-reducing potentiality are big.
Invention content
The present invention generates coking plant sour water and reuse carries out system, global optimization, reduce by adjusting technique
Steam and water resources consumption are implemented sour water tandem and are used, and stripping after-purification water consumption is increased, and sour water is reduced from source
Yield improves sour water and purified water reuse amount, realization device source water-saving and emission-reducing.
Based on this, a kind of optimization coking plant sour water abatement of present invention offer and reuse method comprising：
The first step, selectable control heating furnace steam injection amount；
Second step, selectable control stripper vapor flow of stripper；
Third step may be selected the cold coke of control and operate small steam out and the quantity of steam that steams out greatly；
4th step may be selected to carry out cold coke with stripping the after-purification water section substitute for coke tower steam that steams out greatly；
5th step, may be selected fractionation tower top not water filling or tandem use device sour water makees water filling；
6th step, after the air-cooled preceding rich gas washing water tandem use device sour water of compressor, or use stripping may be selected
Purified water substitutes demineralized water and makees water filling；
7th step may be selected emptying tower top liquid separation tank and drain dual treatment, and initial stage is discharged to out-of-bounds sour water stripping
Device processing, later stage draining are back to coke coke cooling water system water supplement；
8th step may be selected stripping after-purification water and be back to coke coke cooling water system water supplement, and reuse amount is according to system water supplement
Amount demand and field working conditions (such as peculiar smell control) determine.
The first step is specially further that heating furnace tube steam injection uses multiple spot steam injection technology, total injection rate preferably to feed
The 1% of amount can suitably increase injection rate, but be no more than 2% as possible when treating capacity is low.
If the second step is further specifically, fractionating column fractionation wax oil is subsequently into hydrotreating, and wax oil index meets
Hydrotreated feedstock requirement, can cancel steam stripping, if must be stripped, stripped vapor dosage is preferably the 2- of product volume
4%.
Third step is specially further that the cold coke of STRENGTH ON COKE tower is small to steam out, steam out greatly steam according to petroleum coke fugitive constituent
Amount is adjusted, and is implemented the steps reduction of steam injection amount, is reduced the 3%-5% of steam injection amount every time.
4th step is specially further when steaming out cold coke greatly, and acidic water stripping device is net without heat exchange, cooling high temperature
Change water, leading to coke drum from treated water tank purified water pump pressurization steams out greatly operating platform, and mist is respectively enterd with 1.0MPa steam
Change device, purified water and vapour mixture through atomization are sent to coke drum water supply control valve, steam and purification water inventory and original system
Both during which quantity of steam is consistent substantially when all being steamed out greatly with steam, and water ratio is according to tower pressure, tower bottom tower wall temperature
The constraintss such as decrease speed are adjusted, and the two need to be determined finally in the flow of each period by debugging.
5th step is specially further fractionation tower top not water filling as possible, if you need to water filling, will stablize tower top liquid separation tank or
The sour water of rich gas compressor outlet liquid separation tank is introduced directly into fractionation tower top In Oil-gas Line tandem and uses.
6th step is specially further that compressor rich gas washing water directly utilizes fractionation tower top liquid separation tank or stabilizer
It pushes up liquid separation tank sour water or reuse acidic water stripping device is non-plus hydrogen series strips after-purification water, be used as rich gas washing water
Sour water or purified water need to control chloride ion content in water, not more than 100 μ g/g, it is expected that being less than 5 μ g/g.
7th step is specially further that tower top liquid separation tank initial stage sewage send the acidic water stripping device to outside battery limit (BL), and 1
Sewage after hour is discharged into coke cooling water system, is used as coke cooling water system water supplement.
Beneficial effects of the present invention:
Using coking plant sour water proposed by the present invention reduction and reuse method, to coking plant water, draining ring
Section carries out system optimization, reduces steam and water resources consumption, and sour water tandem uses, and reducing sour water from source generates
Amount reduces the sour water amount for entering subsequent acidic water stripper plant, and multipath reuse, which strips after-purification water and reduces, enters sewage
The sewage quantity of Treatment stations end-o f-pipe -control device mitigates acidic water stripping device, end sewage farm pressure, realizes essence cleaning
Production and source water-saving and emission-reducing, can realize the two-win of economic benefit and environmental benefit.
Description of the drawings
Attached drawing 1 is process flow chart after coking plant sour water abatement and reuse optimization.
Specific implementation mode
It includes heating furnace part, coke tower section, fractionating column that coking plant generates related process procedure with sour water
(tower containing steam stripping) part, emptying tower (coke drum steam out emptying) partly, rich tail gas of coking plant compressor section and Vapor recovery unit
Part.Technical process is:Raw material squeezes into coking heater after heat exchange by feed pump, and heating furnace sets steam injection point；Raw material
Enter coke drum bottom through four-way valve after heating, coke drum through it is small steam out, steam out greatly, small water supply, big water supply carry out it is cold it is burnt, cut
It is burnt；Enter with the deep fat gas that top of coke tower flows out with water, heating furnace steam injection, the steam/water of coke drum small period of steaming out in raw material
Fractionating column, it is laggard through water filling, cooling as fractionation tower top oil gas together with the stripped vapor in fractionating column side line steam stripping tower
Enter to be fractionated tower overhead gas liquid liquid separation tank, separates rich tail gas of coking plant, gasoline and sour water；Rich tail gas of coking plant is compressed, washes, after cooling,
Rich gas, gasoline and sour water are isolated through rich gas compression liquid separation tank；Rich gas, gasoline stablize tower overhead gas into absorbing-stabilizing system
Enter Vapor recovery unit liquid separation tank after air-cooled, sour water is discharged.Coke drum steams out greatly, the cold burnt a large amount of high-temperature steams generated and
A small amount of oil gas enters emptying tower, and a large amount of steam of emptying tower top and oil gas enter emptying tower top liquid separation tank, sulfur-bearing is discharged after cooling
Sewage.
A kind of optimization coking plant sour water abatement of present invention offer and reuse method are adjusted relative to traditional handicraft
Whole heating furnace steam injection amount, vapor flow of stripper, it is small steam out and the quantity of steam that steams out greatly, increase the draining of stabilizer liquid separation tank and rich gas compression
Fractionating column waterflood-transmission line is removed in the draining of liquid separation tank, increases the draining of fractionating column liquid separation tank, rich gas washing note is removed in the draining of stabilizer liquid separation tank
Water pipeline increases purified water and mends coke cooling water systematic pipeline, increases emptying tower draining and mends coke cooling water systematic pipeline, increases purified water portion
Point substitute for coke tower steams out greatly steam pipe line and relevant device.
This method further specifically includes：
The first step, selectable control heating furnace steam injection amount.Heating furnace tube steam injection uses multiple spot steam injection technology, total to inject
Amount is preferably the 1% of inlet amount.Treating capacity can suitably increase injection rate when low, but be no more than 2% as possible.It is further reduced usage amount
When, it is contemplated that quantity of steam is adjusted according to exit pressure drop, implements steps reduction, reduces the 3%-5% of steam injection amount every time.
Second step, selectable control stripper vapor flow of stripper.If fractionating column is fractionated wax oil subsequently into hydrotreating, and
Wax oil index meets hydrotreated feedstock requirement, can cancel steam stripping.If must be stripped, stripped vapor dosage is preferably
The 2-4% of product volume, when being further reduced usage amount, it is contemplated that right under conditions of not influencing to produce hydrotreated feedstock requirement
Steam injection amount is adjusted, and implements steps reduction, reduces the 3%-5% of steam injection amount every time.
Third step may be selected the cold coke of control and operate small steam out and the quantity of steam that steams out greatly.Specially foundation petroleum coke fugitive constituent,
The cold coke of STRENGTH ON COKE tower is small to steam out, the quantity of steam that steams out greatly is adjusted, and implements the steps reduction of steam injection amount, reduces steam injection amount every time
3%-5%.
4th step may be selected to carry out cold coke with stripping the after-purification water section substitute for coke tower steam that steams out greatly.It is specially big
When steaming out cold burnt, acidic water stripping device is without heat exchange, cooling high temperature purification water, from the purified water pump pressurization of treated water tank
It leads to coke drum to steam out greatly operating platform, atomizer is respectively enterd with 1.0MPa steam, the purified water through atomization and steam mixing
Object is sent to coke drum water supply control valve, and quantity of steam is protected substantially when steam is all steamed out greatly with steam with purification water inventory with original system
Both during which hold consistent, water ratio is adjusted according to constraintss such as tower pressure, tower bottom tower wall temperature drop rates, need to be led to
Crossing debugging determines the two finally in the flow of each period.When specific debugging, all with steam when general initial, the 5th minute
It plays quantity of steam and rapidly increases to the original steam maximum of system, while being rapidly introduced into a small amount of purified water, can tentatively be set to quantity of steam
10-15% or so, stable operation was by 30 minutes or so.Then it with 5 minutes for interval, gradually decreases quantity of steam, increase purified water
Amount, purification water is adjusted according to constraintss such as tower pressure, tower bottom tower wall temperature drop rates, until purification water and steaming
Vapour amount remains basically stable, and then keeps purification water constant, quantity of steam is gradually decreased, until the end that steams out greatly.Each time control point
And purified water and steam consumption need to determine by debugging repeatedly.
5th step, may be selected fractionation tower top not water filling or tandem use device sour water makees water filling.It is most to be fractionated tower top
Not water filling is measured, if you need to water filling, tower top liquid separation tank will be stablized or rich gas compressor exports the sour water of liquid separation tank and is introduced directly into point
Evaporate the use of tower top In Oil-gas Line tandem.
6th step, after the air-cooled preceding rich gas washing water tandem use device sour water of compressor, or use stripping may be selected
Purified water substitutes demineralized water and makees water filling.Specially compressor rich gas washing water directly using fractionation tower top liquid separation tank or stablizes tower top
Liquid separation tank sour water or reuse acidic water stripping device is non-plus hydrogen series strips after-purification water, as containing for rich gas washing water
Sulphur sewage or purified water need to control chloride ion content in water, not more than 100 μ g/g, it is expected that being less than 5 μ g/g.
7th step may be selected emptying tower top liquid separation tank and drain dual treatment, and initial stage is discharged to out-of-bounds sour water stripping
Device processing, later stage draining are back to coke coke cooling water system water supplement.Specially tower top liquid separation tank initial stage sewage is sent to outside battery limit (BL)
Acidic water stripping device, the sewage after 1 hour is discharged into coke cooling water system, is used as coke cooling water system water supplement.
8th step may be selected stripping after-purification water and be back to coke coke cooling water system water supplement, and reuse amount is according to system water supplement
Amount demand and field working conditions (such as peculiar smell control) determine.
The first step to the 8th step can be adjusted as needed, implement a step or more, in order to obtain abatement and reuse
Maximum, optimum efficiency, it is proposed that synthesis is using each step to obtain overall effect.
Sulfur-bearing of the sour water from generations such as Water entrainment in the feedstock, heating furnace steam injection, stripped vapor, rich gas washing waters is dirty
Water, generating unit mainly have fractionator overhead liquid separation tank, rich gas compressor outlet liquid separation tank, stablize tower top liquid separation tank and emptying tower
Push up liquid separation tank.
Below using embodiment and attached drawing come the embodiment that the present invention will be described in detail, how skill is applied to the present invention whereby
Art means solve technical problem, and the realization process for reaching technique effect can fully understand and implement.
Attached drawing 1 is process flow chart after coking plant sour water abatement and reuse optimization, and main sour water generates, disappears
Subtract and reuse link is as follows：
1) fractionating column liquid separation tank 5., emptying tower liquid separation tank 10., rich gas compress liquid separation tankVapor recovery unit liquid separation tank 14 is dress
Set four positions of sour water generation；
2) 1. heating furnace steam injection amount is adjusted, steam consumption can be reduced, sour water generates.
3) sour water stripping after-purification water 2. can reuse do coke cutting water system water supplement.
4) sour water stripping after-purification water 3. can partial alternative steam out greatly steam.
5) STRENGTH ON COKE tower 4. it is cold it is burnt with it is small steam out, the quantity of steam that steams out greatly is adjusted, reduce steam consumption, sour water production
It is raw.6) coking fractional distillation column 6. tower top not water filling as possible, when needing water filling can tandem compress liquid separation tank using rich gasVapor recovery unit
Liquid separation tankSour water.
7) 7. it is fractionating column wax oil stripper, fractionating column wax oil subsequently meets feed needs into hydrotreating and wax oil index
When, stripping can be cancelled.When must use steam stripping, it is contemplated that right under conditions of not influencing to produce hydrotreated feedstock requirement
Steam injection amount is adjusted, and implements steps reduction, reduces the 3%-5% of steam injection amount every time.
8) 10. initial stage sour water send to acidic water stripping device outside battery limit (BL) and handles emptying tower top liquid separation tank, after 1 hour
2. sewage is discharged into coke cooling water system, be used as coke cooling water system water supplement.
9) rich gas compressor 8. rich gas washing water can directly utilize fractionating column liquid separation tank 5., Vapor recovery unit liquid separation tank 14 contains
Sulphur sewage.
Embodiment 1：
Certain refinery coker designs 2,400,000 t/a of working ability, by being analyzed with water, draining, following optimization can be taken to arrange
It applies：
1) by adjusting heating furnace tube steam injection, ball valve sealing gas and the small quantity of steam that steams out, fractionator overhead sour water
Total amount drops to 7t/h by 10t/h；
2) Vapor recovery unit stabilizer liquid separation tank sour water is back to fractionating column teeming water；
3) purified water substitutes the cold coke that steams out greatly.Device need to be steamed out greatly 2 times daily, and 2.5 hours every time, the amount of steaming out was about
20t/h often handles a tower coke and about needs 1.0MPa steam 45t；Implement purified water replacement, one tower coke of processing only needs about
6t can save 2.8 ten thousand t/a of 1.0MPa steam, 3.3 ten thousand t/a of reuse stripping purification water；
4) atmospheric and vacuum distillation unit sour water tandem is used in the water filling of coking plant rich gas washings, water injection rate 5t/h；
5) purified water is used as coke cooling water system water supplement, about daily 100t of water or so.
By the above Optimized Measures, 5.4 ten thousand t of steam can be saved the device years, sour water yield reduces by 6.2 ten thousand t, only
Change water reuse amount and increases by 6.9 ten thousand t.
Embodiment 2：
Certain 1,400,000 t/a coking plant of refinery, takes following technique adjustment measure：
1) heating furnace steam injection amount is down to 1.8t/h by original 2.4t/h；
2) the small steam consumption that steams out is down to 2.5t/h by 6t/h, and the steam consumption that steams out greatly is down to 11t/h by 20t/h, daily
Save steam 50t；
3) fractionation tower top cancels water filling；
4) it substitutes demineralized water with stripping after-purification water and does rich tail gas of coking plant compressor outlet (before air-cooled) water filling, water injection rate
1.5t/h；
By optimizing and revising above, 2.3 ten thousand t of steam can be saved the device years, sour water yield reduces by 2.3 ten thousand t, only
Change water reuse amount and increases by 1.3 ten thousand t.
Embodiment 3：
Certain 1,600,000 t/a coking plant of refinery takes following Optimized Measures by analyzing device water, draining：
1) heating furnace tube steam injection amount is down to 2t/h by 3t/h；
2) fractionating column wax oil stripper stripped vapor dosage is down to 0.5t/h by 1t/h；
3) the directly whole tandems of the sour water of absorbing-stabilizing system stabilizer liquid separation tank are used in fractionating column teeming water；
4) it substitutes demineralized water with stripping after-purification water and does rich tail gas of coking plant compressor outlet (before air-cooled) water filling, save softened water
And reduce sour water yield 2t/h；
5) small steam out is down to 4t/h by 6t/h, and steam out drops to 12t/h greatly by 20t/h；
6) coke drum steams out greatly original steam consumption as 12t/h, implements purified water and substitutes transformation, first 30 minutes whole use
1.0MPa steam, tolerance are gradually increased to 12t/h, and steam is gradually dropped to 5t/h by 12t/h after 30 minutes, and purified water is gradual from 0
It is added to 7t/h, steam and purified water are with 5 after one hour：7 constant one and a half hours；
7) Partial cleansing water is back to coke cooling water system water supplement, water about 6t/h or so.
After taking the above Optimized Measures, which can reduce 20,000 t/a of steam consumption, according to steam cost per ton
200 yuan of calculating, 4,000,000 yuan/a of escapable cost；5.6 ten thousand t/a of sour water yield can be reduced, according to acidic water stripping device
Processing cost 20 yuan of calculating per ton, 1,120,000 yuan/a of escapable cost；Increase by 50,000 t/a of purified water reuse amount, according to sewage disposal
The 10 yuan of calculating per ton of field processing cost, 500,000 yuan/a of escapable cost.COMPREHENSIVE CALCULATING, by factory's coking plant sour water
Generate and reuse carry out global optimization, year more than 560 ten thousand yuan of escapable cost, remarkable benefit.
All above-mentioned this intellectual properties of primarily implementation, there is no this new products of implementation of setting limitation other forms
And/or new method.Those skilled in the art will utilize this important information, the above modification, to realize similar execution feelings
Condition.But all modifications or transformation belong to the right of reservation based on new product of the present invention.
The above described is only a preferred embodiment of the present invention, being not that the invention has other forms of limitations, appoint
What those skilled in the art changed or be modified as possibly also with the technology contents of the disclosure above equivalent variations etc.
Imitate embodiment.But it is every without departing from technical solution of the present invention content, according to the technical essence of the invention to above example institute
Any simple modification, equivalent variations and the remodeling made, still fall within the protection domain of technical solution of the present invention.
Claims (5)
1. a kind of optimization coking plant sour water abatement and reuse method, which is characterized in that including：
The first step controls heating furnace steam injection amount；
Second step controls stripper vapor flow of stripper；
Third walks, and controls cold coke and operates small steam out and the quantity of steam that steams out greatly；
4th step carries out cold coke with the stripping after-purification water section substitute for coke tower steam that steams out greatly；
5th step, is fractionated tower top not water filling or tandem use device sour water makees water filling；
6th step, the air-cooled preceding rich gas washing water tandem use device sour water of compressor, or substituted using stripping after-purification water
Demineralized water makees water filling；
7th step, emptying tower top liquid separation tank drain dual treatment, and initial stage is discharged to out-of-bounds sulfur-containing sewage stripping device processing, after
Phase draining is back to coke coke cooling water system water supplement；
8th step, stripping after-purification water are back to coke coke cooling water system water supplement, and reuse amount is according to system water supplement amount demand and now
Field operating condition determines；
Further for specially heating furnace tube steam injection using multiple spot steam injection technology, total injection rate is inlet amount to the first step
1%, increase injection rate when treating capacity is low, but be no more than 2%；
Wax oil is fractionated subsequently into hydrotreating, and at wax oil index satisfaction plus hydrogen if the second step is specially further fractionating column
Feed needs are managed, steam stripping is cancelled, if must be stripped, stripped vapor dosage is the 2-4% of product volume；
Third step be specially further according to petroleum coke fugitive constituent the cold coke of STRENGTH ON COKE tower is small to steam out, steam out greatly quantity of steam into
Row adjustment implements the steps reduction of steam injection amount, reduces the 3%-5% of steam injection amount every time.
2. optimization coking plant sour water abatement and reuse method as described in claim 1, it is characterised in that：4th stepping
When one step specially steams out greatly cold burnt, acidic water stripping device is passed through without heat exchange, cooling high temperature purification water from treated water tank
Clarified water pump pressurization leads to coke drum and steams out greatly operating platform, respectively enters atomizer with 1.0MPa steam, the purification through atomization
Water and vapour mixture are sent to coke drum water supply control valve, when steam is all steamed out greatly with steam with purification water inventory with original system
Quantity of steam is consistent substantially, both during which water ratio according to tower pressure, tower bottom tower wall temperature drop rate constraints into
Row adjustment need to determine the two finally in the flow of each period by debugging.
3. optimization coking plant sour water abatement and reuse method as claimed in claim 1 or 2, it is characterised in that：It is described
5th step is specially further fractionation tower top not water filling as possible will stablize tower top liquid separation tank or rich gas compressor goes out if you need to water filling
The sour water of mouth liquid separation tank is introduced directly into fractionation tower top In Oil-gas Line tandem and uses.
4. optimization coking plant sour water abatement and reuse method as claimed in claim 1 or 2, it is characterised in that：It is described
6th step is specially further that compressor rich gas washing water directly utilizes fractionation tower top liquid separation tank or stable tower top liquid separation tank sulfur-bearing
Sewage or reuse acidic water stripping device is non-plus hydrogen series strips after-purification water, is used as the sour water or net of rich gas washing water
Change water, chloride ion content in water, not more than 100 μ g/g need to be controlled, it is expected that being less than 5 μ g/g.
5. optimization coking plant sour water abatement and reuse method as claimed in claim 1 or 2, it is characterised in that：It is described
7th step is specially further that tower top liquid separation tank initial stage sewage send the acidic water stripping device to outside battery limit (BL), the sewage after 1 hour
It is discharged into coke cooling water system, is used as coke cooling water system water supplement.
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| CN108793295B (en) * | 2017-05-02 | 2021-06-25 | 中国石油化工股份有限公司 | Method for reducing and recycling sulfur-containing sewage of oil refinery |
| CN112939358B (en) * | 2021-02-05 | 2021-11-26 | 内蒙古包钢集团环境工程研究院有限公司 | Phenol-cyanogen wastewater reduction method |
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