CN109381887A - The pretreatment system and method for the high ammonia nitrogen acidity condensate liquid of converter unit - Google Patents
The pretreatment system and method for the high ammonia nitrogen acidity condensate liquid of converter unit Download PDFInfo
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- CN109381887A CN109381887A CN201710655329.5A CN201710655329A CN109381887A CN 109381887 A CN109381887 A CN 109381887A CN 201710655329 A CN201710655329 A CN 201710655329A CN 109381887 A CN109381887 A CN 109381887A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0005—Degasification of liquids with one or more auxiliary substances
- B01D19/001—Degasification of liquids with one or more auxiliary substances by bubbling steam through the liquid
- B01D19/0015—Degasification of liquids with one or more auxiliary substances by bubbling steam through the liquid in contact columns containing plates, grids or other filling elements
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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Abstract
The invention belongs to coal chemical industrial waste waters, exhaust-gas treatment field, and in particular to the high ammonia nitrogen acidity condensate liquid pretreatment system of converter unit and method.Coal gasification converter unit Heat Exchanger in Circulating Water System is changed to desalination water- to-water heat exchanger by the present invention, Circulating Water Field load is reduced while making heating agent recycling heat using desalted water, knockout tower entrance stripping liquid temperature is turned up to 100 DEG C~138 DEG C, acid condensate liquid (containing high ammonia nitrogen) stain disease is pre-processed in knockout tower using class steam stripping method, dissolved gas (the high ammonia nitrogen substances etc.) gasification separation as far as possible in its liquid phase is made.The result shows that: high ammonia nitrogen substances, organic matter and sulfur-containing compound total amount in gas phase are significantly increased, and liquid phase finally enters biochemical unit with the low total amount less than 50kg/h, the processing load for having reached biochemical unit, thereby ensures that the qualified discharge after biochemical treatment.
Description
Technical field:
The invention belongs to coal chemical industrial waste waters, exhaust-gas treatment field, and in particular to the high ammonia nitrogen acidity condensate liquid of converter unit is pre-
Processing system and method.
Technical background:
Ammonia nitrogen stain disease has great harm to natural environment, human body etc..The main harm of ammonia and nitrogen pollution are as follows: make water body just
Normal dissolution oxygen balance is interfered, and further results in water quality deterioration；Source quality is influenced, water process burden is increased；Accelerate
Water eutrophication process.
The improvement of high ammonia nitrogen stain disease is enterprise's urgent need to solve the problem.By concentration difference, ammonia nitrogen stain disease is divided into 3
Class: (1) ammonia nitrogen in high density stain disease: NH3-N>500mg/L；(2) intermediate concentration ammonia nitrogen stain disease: NH3- N is 50~500mg/L；
(3) low-concentration ammonia-nitrogen stain disease: NH3-N<50mg/L。
The high ammonia nitrogen acidity condensate liquid of coal gasification apparatus converter unit, contains a certain amount of NH3、CO2、Cl-1、
、H2The components such as S are needed by pretreatment, preprocess method is by condensate liquid vapour before sending biochemical device to handle
Processing is proposed, i.e., condensate liquid is first stripped with stripping tower, stripping tail gas is cooled to 50~60 DEG C through heat exchanger, subsequently into gas-liquid separation
Tower, separation top are routed directly to acid torch burning, and a kind of separation approach of tower bottom lime set is to send to coal mill system, another way
Diameter is to send to handle in biochemical wastewater treatment pond；As the converter unit of certain gasifying powder coal device uses low liquid to steam ratio technique, technique
Condensate liquid stripper exports gas phase after the separation of stripper knockout tower, and methanol wastewater converges in the high-ammonia-nitrogen sewage and system of about 2t/h
Sewage-treatment plant is sent in conjunction.Due to sulfide in this strand of stain disease and the equal superelevation of ammonia nitrogen, COD, NH sometimes3- N is up to 10
000mg/L or more easily causes to impact to the treatment process of biochemical stain disease, causes outlet total ammonia nitrogen, COD cannot row up to standard
It puts.In addition in condensation process, when temperature reduces, CO2Ammonium salt crystallization object is easily generated with ammonia, causes entire pipeline and condensed system
The blocking of system, while also there is biggish corrosivity to pipeline.And for giving for coal mill system, due to the high ammonia in condensate liquid
To the inlet and outlet pipeline of fire pump, the ammonia nitrogen value in addition also resulting in externally discharged waste water is higher for nitrogen content, easily blocking grinding machine, up to not
Environmentally friendly emission request till now.
Patent (CN 2016112029419) discloses conversion gas condensate liquid recycling system in a kind of Ammonia Production,
Conversion gas condensate liquid after once stripping is subjected to secondary stripping, the conversion gas condensate liquid after secondary stripping contains ammonia
Nitrogen compound, sulfur-containing compound content be effectively reduced, the conversion gas condensate liquid after the secondary stripping is sent can be effective to grinding machine
Improve the working environment of coal-grinding slurrying workshop section, solves the inlet/outlet pipeline blockage problem of grinding machine feed pump, guarantee the stabilization of slurrying
With raising coal-water fluid concentration, improve the water quality of subsequent gasification system.
Patent (ZL 200910098944.6) discloses the gas stripping process of process condensate in a kind of CO transformation, to understand
Certainly ammonium salt crystallization blockage problem occurs for conversion process condensate liquid stripping system, uses two strippers respectively to CO2And NH3
It is stripped, avoids CO2And NH3A possibility that existing simultaneously in systems extends the week of converting means stable operation
Phase, but it does not solve the problems, such as pipeline, equipment blocking and corrosion fundamentally.
But the solution of the above patent is solved the problems, such as by way of increasing stripping tower, two-tower process, not only
Increase the complexity of processing technology, uncontrollability, and is also added significantly to cost, while occupying place.
Summary of the invention
In view of the deficiencies of the prior art, it is an object of the present invention to provide a kind of high ammonia nitrogen acidity condensations of converter unit
Liquid treating system, the system and device is simple, and cost of investment is low.
It is another object of the present invention to provide the high ammonia nitrogen acidity condensate liquid preprocess methods of converter unit, using this hair
Bright pretreatment system has the ammonia nitrogen of relatively low amount by this method knockout tower liquid phase, meets biochemical unit water inlet standard, through life
It, can qualified discharge after change processing.
The high ammonia nitrogen acidity of converter unit of the present invention condenses liquid treating system, including stripper 1, heat exchanger 2, knockout tower 3；
1 top of stripper is equipped with the import of converter unit condensate liquid, and stripping offgas outlet is equipped at the top of stripper 1；Institute
Stripping offgas outlet is stated to be connected with 2 tube-side inlet of heat exchanger；
The heat exchanger 2 is U-tube heat exchanger 2, is equipped with tube side entrance and shell side entrance, in tube-side inlet pipeline and
Tube side outlet line is equipped with bypass, and bypass is equipped with bypass valve 4, and temperature control valve (TCV) 5 is equipped at shell-side outlet；
The knockout tower 3 is equipped with entrance and is connected with the outlet of the tube side of heat exchanger 2, and outlet is equipped at the top of knockout tower 3, passes through pipe
Line is connected with sour gas flare system, and pressure regulator valve 7 is equipped on outlet line, and 3 bottom of knockout tower is equipped with outlet and passes through pipeline
It is connected with gasification installation storage tank, Liquid level adjusting valve 8 is equipped on outlet line.
Preferably, the outlet of knockout tower 3 connects two-way pipeline to flare system.
Preferably, 3 equipment material of knockout tower is 321 material of stainless steel.
Preferably, spare pressure regulator valve 6 is additionally provided on the outlet line.
Preferably, heat preservation substance is surrounded by knockout tower 3 and the pipeline of acid flare system.
The high ammonia nitrogen acidity condensation liquid processing method of converter unit of the present invention includes the following steps: using above system
1) conversion gas condensate liquid enters in stripper 1 from 1 top of stripper, ammonia and sour gas stripping in condensate liquid
Out, stripping gas passes through going out after foam removal from 1 top exit of stripper for 1 top of stripper, and a part of gas passes through pipeline
Into in heat exchanger 2, a part of gas is directly entered in knockout tower 3 from bypass；The stripping gas of 1 top exit of stripper
Temperature is 140~148 DEG C；
2) into the stripping gas of heat exchanger 2 by heat exchanger 2, enter pipeline after cooling, and the stripping gas passed through from bypass,
Enter in knockout tower 3 together, control 3 entrance of knockout tower stripping liquid temperature is 100 DEG C~138 DEG C, and the cooling of the heat exchanger 2 is situated between
Matter is desalted water；
3) gas-liquid separation in knockout tower 3, gas phase go sour gas flare system to burn after pressure regulator valve 7 adjusts exhaust gas phase pressure
Burning processing；Liquid phase enters gasification stain disease point after entering gasification installation storage tank after Liquid level adjusting valve 8 adjusts the liquid level of knockout tower 3
From system.
In technical solution of the present invention, stripping gas walks tube side in heat exchanger 2, and desalted water walks shell side in heat exchanger 2.
In technical solution of the present invention, the temperature control valve (TCV) 5 of shell-side outlet is used to measure the desalination coolant-temperature gage after heat exchange, leads to
The temperature and flow for crossing shell-side outlet desalted water, feed back the temperature of tube side outlet stripping gas out, then regulate and control opening for bypass valve 4
Mouthful.
Preferably, the desalted water for having passed through 2 tube side of heat exchanger in the step 2) is used for the supply of boiler water.Using desalination
Water not only alleviates the burden of Circulating Water Field, and its supply for being used for boiler water, realizes the recycling of heat and resource.
Preferably, in the step 2), control 3 entrance of knockout tower stripping liquid temperature is 115~138 DEG C.
Preferably, in the step 3), adjustment exhaust gas phase pressure is 0.35~0.38MPa.
Preferably, in the step 3), the Liquid level of knockout tower 3 is strip tower height degree 40~60%.
The high ammonia nitrogen acidity condensate liquid preprocess method of converter unit of the present invention, in step 3), liquid phase is less than 50kg/h's
Amount of acidic substances enters biochemical unit.
The principle of the invention and advantage:
The present invention mainly utilizes class steam stripping method principle, and it is according to ammonia in liquid that ammonia vaporizing extract process, which belongs to physical treatment process,
Mutually different with dissolubility in gas phase come what is carried out, it is a mass transport process, i.e., at high operating temperatures, reduces ammonia nitrogen in stain disease
The method of concentration.Difference in partial pressure and waste water of its motive force from ammonia in air between the comparable equilibrium partial pressure of ammonia density, makes
Gas dissolved water and volatile solutes pass through gas-liquid interface, shift to gas phase, and ammonia nitrogen concentration reduces in stain disease, to reach
Remove the purpose of pollutant.Class steam stripping method is on the basis of vaporizing extract process according to coal chemical engineering equipment process characteristic, converter unit
Gas phase heat exchange after medium temperature be still greater than 100 DEG C, do not needed in knockout tower it is outer draw heat source (steam), gas-liquid is directly divided
From the ammonia nitrogen in stain disease is separated.
Since the ammonia nitrogen in stain disease is usually with ammonium ion (NH4+) and free ammonia (NH3) state keep balance and exist,
The equilibrium relation in stain disease are as follows: NH4++ OH-=NH3+H20.In knockout tower, gas phase is communicated with flare line, and pressure is close
Atmospheric pressure, according to Dalton's law (of partial pressures), partial pressure of the solute gas on liquid level is substantially reduced with the decompression of gas；According to
Henry's law, since the partial pressure of solute gas on liquid level reduces, to keep vapor liquid equilibrium, the ammonia dissolved in water constantly escapes from liquid phase
Enter gas phase out, so that ammonia nitrogen concentration in stain disease is formed the reduction of direct ratio as partial pressure reduces, therefore separated by control
Journey is removed ammonia volatilization evolution therein as gas.
The present invention improves the Heat Exchanger in Circulating Water System of the prior art, setting bypass, and by temperature control valve (TCV), precisely
Regulating and controlling temperature, the temperature of control knockout tower entrance are 100~138 DEG C, since temperature is greater than 100 DEG C, are not needed in knockout tower
Draw heat source (steam) outside, gas-liquid is directly separated, and the ammonia nitrogen in stain disease is largely efficiently separated into gas phase, that is, is being saved
Under about a large amount of energy scenario, efficient separating effect can be but generated.
When being handled using the high ammonia nitrogen condensate liquid of prior art progress coal gasification converter unit, liquid phase acidic substance content
Amount greater than 240kg/h, since waste strength is excessively high, is brought huge after carrying out biochemical system to the processing of biochemical system
Impact, and the waste liquid that can not form environment protection standard is discharged, through the invention after technological improvement, process condensate of the invention
Liquid, high ammonia nitrogen substances, waste organic matter and a large amount of gasification separations of sulfur-containing compound in acid condensate liquid sewage after stripping, finally with
Enter biochemical unit less than 50kg/h amount of acidic substances, reduce biochemical treatment amount, it is possible thereby to guarantee the waste water of outlet with
It, can qualified discharge after biochemical treatment after the waste water mixing that methanol comes.
In addition, the present invention is desalted water used in the heat exchanger, the corrosiveness of heat exchanging device is effectively avoided, no
Only first mate alleviates the burden of Circulating Water Field, and its supply for being used for boiler water, realizes effective recycling of heat and resource
It utilizes.
The present invention has done Insulation to removing torch systematic pipeline, it is ensured that does not generate ammonium in going torch systematic procedure
Salt crystal avoids the blocking to pipeline.
Process unit of the invention is simple, and without increasing place land occupation, cost of investment is low, process, easy to operate, and
The emission problem of stain disease in the high ammonia nitrogen condensate liquid pretreatment of current converter unit is efficiently solved, while the present invention is in technique mistake
Cleverly benefit has class steam stripping principle in journey, is effectively saved the energy.Technique of the invention can be promoted in coal chemical technology
It is practical, facilitation can be played to the development of coal chemical industry.
Detailed description of the invention:
Attached drawing 1 is that the high ammonia nitrogen acidity of converter unit condenses liquid treating system
In Fig. 1: 1, stripper；2, heat exchanger；3, knockout tower；4, bypass valve；5, temperature control valve (TCV)；6, spare pressure regulation
Valve；7, pressure regulator valve；8, Liquid level adjusting valve.
Specific embodiment:
Following embodiment is intended to further illustrate the content of present invention, rather than limits the protection model of the claims in the present invention
It encloses.
The high ammonia nitrogen acidity condensation liquid treating system of converter unit is as shown in the figure: including stripper 1, heat exchanger 2, knockout tower 3；
1 top of stripper is equipped with the import of converter unit condensate liquid, and stripping offgas outlet is equipped at the top of stripper 1；The stripping tail
Gas outlet is connected with 2 tube-side inlet of heat exchanger；The heat exchanger 2 is U-tube heat exchanger 2, is gone out equipped with tube side entrance and shell side
Entrance is equipped with bypass on tube-side inlet pipeline and tube side outlet line, and bypass is equipped with bypass valve 4, in shell-side outlet
Place is equipped with temperature control valve (TCV) 5；The knockout tower 3 is equipped with entrance and is connected with the outlet of the tube side of heat exchanger 2, is equipped at the top of knockout tower 3
Outlet, is connected by pipeline with sour gas flare system, and pressure regulator valve 7 is equipped on outlet line, and 3 bottom of knockout tower is equipped with
Mouth is connected by pipeline with gasification installation storage tank, and Liquid level adjusting valve 8 is equipped on outlet line.The outlet of knockout tower 3 connection
Two-way pipeline is to flare system.3 equipment material of knockout tower is 321 material of stainless steel.It is additionally provided on the outlet line standby
With pressure regulator valve 6.Heat preservation substance is surrounded by knockout tower 3 and the pipeline of acid flare system.
Embodiment 1
Conversion gas condensate liquid enters in stripper from 1 top of stripper, and the sour gas in condensate liquid is stripped out, vapour
Mention gas across the top of stripper 1 after foam removal from 1 top exit of stripper, into the pipeline being connected with heat exchanger 2, the vapour
The temperature of the stripping gas of 1 top exit of stripper is 148 DEG C.
Stripping gas passes through the tube side of heat exchanger 2, and the desalted water for being entered shell side is cooled down, with the stripping passed through from bypass
Gas enters in knockout tower together, and control knockout tower entrance stripping liquid temperature is 135 DEG C；It is described to pass through shell side desalted water access tube
Line carries out boiler replenishing water；
Cooled stripping liquid enters in knockout tower, and the gas-liquid separation in knockout tower, gas phase adjusts exhaust gas through pressure regulator valve
Phase pressure is 0.35MPa；After go sour gas flare system burning disposal；Liquid phase adjusts the liquid level of knockout tower through Liquid level adjusting valve 8
It is 40%, enters gasification stain disease separation system after entering gasification installation storage tank afterwards.Its gas phase and liquid phase amount of acidic substances
Detection is shown in Table 1.
Embodiment 2
Conversion gas condensate liquid enters in stripper from stripper top, and the sour gas in condensate liquid is stripped out, vapour
It mentions gas and is exported after foam removal from stripper top across stripper top, into the pipeline being connected with heat exchanger, the stripping
The temperature of the stripping gas of top of tower outlet is 146 DEG C.
Stripping gas passes through the tube side of heat exchanger 2, and the desalted water for being entered shell side is cooled down, with the stripping passed through from bypass
Gas enters in knockout tower together, and control knockout tower entrance stripping liquid temperature is 138 DEG C；It is described to pass through shell side desalted water access tube
Line carries out boiler replenishing water；
Cooled stripping liquid enters in knockout tower, and the gas-liquid separation in knockout tower, gas phase adjusts exhaust gas through pressure regulator valve
Phase pressure is 0.37MPa；After go sour gas flare system burning disposal；Liquid phase adjusts the liquid level of knockout tower through Liquid level adjusting valve 8
It is 50%；Enter gasification stain disease separation system after entering gasification installation storage tank afterwards.Its gas phase and liquid phase amount of acidic substances
Detection is shown in Table 1.
Embodiment 3
Conversion gas condensate liquid enters in stripper from stripper top, and the sour gas in condensate liquid is stripped out, vapour
It mentions gas and is exported after foam removal from stripper top across stripper top, into the pipeline being connected with heat exchanger, the stripping
The temperature of the stripping gas of top of tower outlet is 140 DEG C.
Stripping gas passes through the tube side of heat exchanger 2, and the desalted water for being entered shell side is cooled down, with the stripping passed through from bypass
Gas enters in knockout tower together, and control knockout tower entrance stripping liquid temperature is 105 DEG C；It is described to pass through shell side desalted water access tube
Line carries out boiler replenishing water；
Cooled stripping liquid enters in knockout tower, and the gas-liquid separation in knockout tower, gas phase adjusts exhaust gas through pressure regulator valve
Phase pressure is 0.37MPa；After go sour gas flare system burning disposal；Liquid phase adjusts the liquid level of knockout tower through Liquid level adjusting valve 8
It is 60%；Enter gasification stain disease separation system after entering gasification installation storage tank afterwards.Its gas phase and liquid phase amount of acidic substances
Detection is shown in Table 2.
Comparative example 1
Conversion gas condensate liquid enters in stripper from stripper top, and the sour gas in condensate liquid is stripped out, vapour
It mentions gas and is exported after foam removal from stripper top across stripper top, into the pipeline being connected with heat exchanger, the stripping
The temperature of the stripping gas of top of tower outlet is 148 DEG C.
Stripping gas passes through the tube side of heat exchanger 2, and the recirculated water for being entered shell side is cooled down, after circulating water, condensation
Stripping liquid be 75 DEG C
Cooled stripping liquid enters in knockout tower, and the gas-liquid separation in knockout tower, gas phase adjusts exhaust gas through pressure regulator valve
Phase pressure is 0.38；After go sour gas flare system burning disposal；The liquid level that liquid phase adjusts knockout tower through Liquid level adjusting valve 8 is laggard
Enter gasification stain disease separation system after entering gasification installation storage tank.The detection of its gas phase and liquid phase amount of acidic substances is shown in Table 2.
1 Examples 1 to 2 of table separates/liquid phase composition of working off one's feeling vent one's spleen
As can be seen from the table, 135 DEG C of liquid phase total amount is 27.0kgh-1, and 138 DEG C of liquid phase total amount be even more down to
9kg·h-1, significantly reduce biochemical treatment amount.
2 embodiment 3 of table, comparative example 1 separate/liquid phase composition of working off one's feeling vent one's spleen
As can be seen from the table, 1 092.3kg/h when the total amount of gas phase is from 75 DEG C is increased to 1 at 105 DEG C
282.2kg/h；In liquid phase total amount then from 75 DEG C when 44.8kg/h of 234.7kg/h when dropping to 105 DEG C, it is possible thereby to guarantee
The waste water of outlet biochemical unit meets biochemical unit processing standard can qualified discharge after biochemical treatment.
Claims (12)
1. the high ammonia nitrogen acidity of converter unit condenses liquid treating system, including stripper (1), heat exchanger (2), knockout tower (3)；It is described
Stripper (1) top is equipped with the import of converter unit condensate liquid, and stripping offgas outlet is equipped at the top of stripper (1)；The stripping tail
Gas outlet is connected with heat exchanger (2) tube-side inlet；It is characterized by:
The heat exchanger (2) is U-tube heat exchanger (2), is equipped with tube side entrance and shell side entrance, in tube-side inlet pipeline and
Tube side outlet line is equipped with bypass, and bypass is equipped with bypass valve (4), is equipped with temperature control valve (TCV) (5) at shell-side outlet；
The knockout tower (3) is equipped with entrance and is connected with the outlet of the tube side of heat exchanger (2), and outlet is equipped at the top of knockout tower (3), is passed through
Pipeline is connected with sour gas flare system, is equipped with pressure regulator valve (7) on outlet line, and it is logical that knockout tower (3) bottom is equipped with outlet
It crosses pipeline to be connected with gasification installation storage tank, is equipped with Liquid level adjusting valve (8) on outlet line.
2. the high ammonia nitrogen acidity of converter unit according to claim 1 condenses liquid treating system, it is characterised in that: the separation
Tower (3) outlet connects two-way pipeline to flare system.
3. the high ammonia nitrogen acidity of converter unit according to claim 1 condenses liquid treating system, it is characterised in that: the separation
Tower (3) equipment material is 321 material of stainless steel.
4. the high ammonia nitrogen acidity of converter unit according to claim 1 condenses liquid treating system, it is characterised in that: the outlet
Spare pressure regulator valve (6) are additionally provided on pipeline.
5. the high ammonia nitrogen acidity of converter unit according to claim 1 condenses liquid treating system, it is characterised in that: in knockout tower
(3) heat preservation substance is surrounded by on the pipeline of acid flare system.
6. the high ammonia nitrogen acidity of converter unit condenses liquid processing method, using the system as described in Claims 1 to 5, feature exists
In including the following steps:
1) conversion gas condensate liquid enters in stripper (1) from stripper (1) top, ammonia and sour gas stripping in condensate liquid
Out, stripping gas passes through goes out after foam removal from stripper (1) top exit at the top of stripper (1), and a part of gas passes through
Pipeline enters in heat exchanger (2), and a part of gas is directly entered in knockout tower (3) from bypass；Stripper (1) top exit
Stripping gas temperature be 140~148 DEG C；
2) into the stripping gas of heat exchanger by heat exchanger (2), enter pipeline after cooling, and the stripping gas passed through from bypass, one
Rise enter knockout tower (3) in, control knockout tower (3) entrance stripping liquid temperature be 100 DEG C~138 DEG C, the heat exchanger (2) it is cold
But medium is desalted water；
3) gas-liquid separation in knockout tower (2), gas phase go sour gas flare system to burn after pressure regulator valve (7) adjust exhaust gas phase pressure
Burning processing；Liquid phase enters dirty give up of gasifying after entering gasification installation storage tank after Liquid level adjusting valve (8) adjust the liquid level of knockout tower (2)
Water separating system.
7. the high ammonia nitrogen acidity of converter unit according to claim 6 condenses liquid processing method, it is characterised in that: the shell side
The temperature control valve (TCV) (5) of outlet is used to measure the temperature of the desalted water after heat exchange, passes through the temperature and stream of shell-side outlet desalted water
Amount, feeds back the temperature of tube side outlet stripping gas out, then regulates and controls the opening of bypass valve (4).
8. the high ammonia nitrogen acidity of converter unit according to claim 7 condenses liquid processing method, it is characterised in that: the step
2) desalted water for having passed through heat exchanger shell pass in is used for the supply of boiler water.
9. the high ammonia nitrogen acidity of converter unit according to claim 6 condenses liquid processing method, it is characterised in that: the step
2) in, control knockout tower (3) entrance stripping liquid temperature is 115~138 DEG C.
10. the high ammonia nitrogen acidity of converter unit according to claim 6 condenses liquid processing method, it is characterised in that: the step
It is rapid 3) in, adjustment exhaust gas phase pressure be 0.35~0.38MPa.
11. the high ammonia nitrogen acidity of converter unit according to claim 6 condenses liquid processing method, it is characterised in that: the step
It is rapid 3) in, the Liquid level of knockout tower (3) be strip tower height degree 40~60%.
12. the high ammonia nitrogen acidity of converter unit according to claim 6 condenses liquid processing method, it is characterised in that: the step
It is rapid 3) in, liquid phase is to enter biochemical unit less than the amount of acidic substances of 50kg/h.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111744227A (en) * | 2020-07-30 | 2020-10-09 | 东华工程科技股份有限公司 | Steam stripping process for low-temperature condensate in coal chemical conversion |
| CN112856912A (en) * | 2021-01-29 | 2021-05-28 | 山西沃能化工科技有限公司 | Method for saving water for evaporative cooling device |
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| CN102502901A (en) * | 2011-09-23 | 2012-06-20 | 中国石油化工股份有限公司 | Condensed fluid stripping method matched with CO transforming device |
| CN103058295A (en) * | 2012-12-19 | 2013-04-24 | 中国五环工程有限公司 | Technology of low pressure steam stripping shift conversion technical condensed fluid |
| CN203474575U (en) * | 2013-03-13 | 2014-03-12 | 武汉宏澳绿色能源工程有限责任公司 | Equipment system for coal gasification wastewater chemical engineering separation |
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| CN106082379A (en) * | 2016-07-27 | 2016-11-09 | 青岛科技大学 | The method that stripping contains ammonia wastewater from chemical industry containing acid |
| CN106524822A (en) * | 2016-09-28 | 2017-03-22 | 中国航空规划设计研究总院有限公司 | Liquid mixing and temperature adjusting method of cooling process of heat transformation |
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| CN111744227A (en) * | 2020-07-30 | 2020-10-09 | 东华工程科技股份有限公司 | Steam stripping process for low-temperature condensate in coal chemical conversion |
| CN111744227B (en) * | 2020-07-30 | 2022-03-04 | 东华工程科技股份有限公司 | Steam stripping process for low-temperature condensate in coal chemical conversion |
| CN112856912A (en) * | 2021-01-29 | 2021-05-28 | 山西沃能化工科技有限公司 | Method for saving water for evaporative cooling device |
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