CN110171857A - A kind of graywater treating method of coal slurry gasification containing ammonium hydroxide - Google Patents
A kind of graywater treating method of coal slurry gasification containing ammonium hydroxide Download PDFInfo
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- CN110171857A CN110171857A CN201910316708.0A CN201910316708A CN110171857A CN 110171857 A CN110171857 A CN 110171857A CN 201910316708 A CN201910316708 A CN 201910316708A CN 110171857 A CN110171857 A CN 110171857A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
-
- 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
-
- 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
- C02F1/048—Purification of waste water by evaporation
-
- 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
- C02F1/06—Flash evaporation
-
- 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
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
The present invention relates to a kind of graywater treating methods of coal slurry gasification containing ammonium hydroxide, it is characterized by comprising following step: tower and the flashed vapour progress Hybrid Heating from tower under first on first are sent into after buck, enter tower on second after being forced into 0.2~0.4MPaG, it is mixed with the flashed vapour from the second lower tower, stripper is entered after pressurization and is stripped；Stripping gas is low-pressure steam and fixed gas；Fixed gas is by injector injection to the stripper；The buck of stripper tower bottom sequentially enters the second lower tower, the first lower tower carries out full flashing and secondary flash, and the flash steam after flash distillation recycles heat, and the liquid phase generated after secondary flash sends to downstream wastewater processing unit.The present invention solves the problems, such as that the device cycle of operation caused by fouling of heat exchangers, blocking is short, reduces plant energy consumption and operating cost.
Description
Technical field
The present invention relates to field of waste water treatment, more particularly to a kind of graywater treating method of coal slurry gasification containing ammonium hydroxide.
Background technique
The chilled water being discharged in coal water slurry gasifying device gasification furnace passes through high pressure flash, low pressure flash, the first vacuum flashing
After recycling heat with the second vacuum flashing, then stripping system removing most ammonia-nitrogen is sent into after flocculation, coagulating sedimentation and is sent to entirely
Factory's sewage-treatment plant.Buck after flocculation, coagulating sedimentation easily leads to heat exchanger, vapour since calcium ions and magnesium ions are relatively high
Stripper disk and related pipeline scaling problem, influence the long period stable operation of stripper plant, increase parking process number, cost
It is dangerous with safety wind.
Summary of the invention
There is provided the technical problem to be solved by the present invention is to the status for the prior art a kind of can effectively slow down dirty layer
Synthesis speed, to extend the graywater treating method of coal slurry gasification containing ammonium hydroxide of stable operation cycle.
The technical scheme of the invention to solve the technical problem is: a kind of ash of coal slurry gasification containing ammonium hydroxide water process side
Method, it is characterised in that include the following steps:
Buck after flocculant, coagulant and lye agent-feeding treatment qualification is pressurized to 0.3~0.5MPaG and is sent into first
Upper tower is that the secondary flash gas that 95~105 DEG C of pressure are 0~0.1MPaG carries out Hybrid Heating with the temperature from the first lower tower,
On first tower bottom of tower obtain temperature be 70~80 DEG C, pressure be the logistics of -0.05~-0.02MPaG mixed once；Control institute
Stating the operating pressure on first in tower is -0.05~-0.02MPaG；
Mixed once logistics enters tower on second after being forced into 0.2~0.4MPaG, is with the temperature from the second lower tower
110~120 DEG C of pressure are that 0.15~0.2MPaG full flashing gas is mixed, and it is 100 that the tower bottom of tower, which obtains temperature, on second
~110 DEG C, the secondary mixture stream that pressure is 0.05~0.1MPaG；Control tower on described second operating pressure be 0.05~
0.1MPaG；
Secondary mixture stream is stripped after being forced into 0.5~0.6MPaG into stripper；Used in the stripper
Stripping gas is from 0.3~0.5MPaG, 180 ± 5 DEG C of low-pressure steam and the tower and described second on described first out-of-bounds
The fixed gas of upper tower；The fixed gas is by injector injection to the stripper；The operating pressure for controlling the stripper is 0.2
~0.4MPaG, temperature are 131~150 DEG C；
After stripping, the mixture of tower top the discharge ammonia and vapor of the stripper, the mixture generates after processing
Fixed gas send sulfur recovery unit or torch burning, ammonium hydroxide generated is divided into two strands, wherein first strand of ammonium hydroxide returns to the vapour
Stripper carries out reflux operation, and second strand of ammonium hydroxide is sent out out-of-bounds as ammonium hydroxide product；
The buck that the stripper tower bottom pressure is 0.3~0.4MPaG enters the second lower tower using pressure difference and is once dodged
It steams, the operating pressure for controlling the described second lower tower is 0.1~0.2MPaG, and the full flashing vapour generated after full flashing is as warm
Source enters tower on described second and heats primary mixture；
The liquid phase obtained after full flashing is pressurized to 0.1~0.3MPaG and send to the described first lower tower progress secondary flash, control
The operating pressure made in the described first lower tower is 0~0.1MPaG；The gas phase generated after secondary flash enters tower on described first and makees
The buck is heated for heat source, obtains primary mixture；
The liquid phase generated after secondary flash sends to downstream wastewater processing unit.
It is preferred that the gas phase that the temperature of the stripper overhead discharge is 125~135 DEG C enters back after being cooled to 40~45 DEG C
Stream tank is cached, while isolating the fixed gas；The ammonium hydroxide of the generation is drawn through reflux pump, by controlling reflux pump
Flow control outlet ammonia concn is 15%wt.
It is preferred that the qualified ash of the described first lower tower discharge sends to downstream wastewater processing unit after being water-cooled to 40~50 DEG C.
As the further improvement of above-mentioned each scheme, tower and the first lower tower share the first tower on preferably described first
Body, the first lower tower pass through tower in the first gas-phase transport pipeline connection first；The first gas-phase transport pipeline is located at described first
Outside tower body, the entrance of the first gas-phase transport pipeline is located at the top of the first lower tower, and the outlet of the first gas-phase transport pipeline is located at the
The middle part of tower on one；
Tower and the second lower tower share the second tower body on described second, and the second lower tower is connected by the second gas-phase transport pipeline
Connect tower on second；The second gas-phase transport pipeline is located at outside second tower body, and the entrance of the second gas-phase transport pipeline is located at
The top of second lower tower, the outlet of the second gas-phase transport pipeline are located at the middle part of tower on second.It is long that the program can shorten pipeline
It spends, thermal loss is small during logistics delivery.
It is preferred that tower is solid valve-type tower tray tower on tower and described second on described first, the quantity of tower tray is 3-5 block.
As the further improvement of above-mentioned each scheme, the pressure difference on preferably described first between tower and the first lower tower is
50-100kPa；Pressure difference on described second between tower and the second lower tower is 50-100kPa；To be more conducive to gas phase in lower tower
Automatic flowing, while guaranteeing the flash evaporation effect of lower tower.
The amount for entering the low-pressure steam in stripper in above-mentioned each scheme can be according to buck situation to be processed and processing
The requirement of ammonia-nitrogen content determines in after-purification buck, consumption reduction, and the amount that the stripper is passed through low-pressure steam is object to be stripped
8~10v% of material.
In above-mentioned each scheme, the buck to be processed passes through flocculant, coagulant and lye agent-feeding treatment, can be according to need
The prior art is selected, preferably, the buck to be processed is after flocculant, coagulant and lye agent-feeding treatment qualification, place
In i.e. normal temperature and pressure and pH value is greater than 12.
Compared with prior art, the present invention is avoided using the high temperature gas-phase heating buck to be processed generated after the flash distillation of lower tower
Heat exchanger is used, the short problem of device cycle of operation caused by fouling of heat exchangers, blocking, and sufficiently benefit are not only solved
With system thermal, plant energy consumption and operating cost are reduced；The heat exchange mode directly contacted using liquid phase simultaneously, heat transfer temperature
Poor big, Mass and heat transfer is high-efficient, whole tower operating space with respect to heat exchanger tube or nozzle for, will not influence to change because of a small amount of dirty layer
The thermal efficiency can extend device operation cycle and NH_3-N treating index stability with high degree；Simultaneously by tower on two evaporating columns
The fixed gas isolated is sent to stripper as heat source, saves stripped vapor consumption.
Detailed description of the invention
Fig. 1 is flow chart of the embodiment of the present invention.
Specific embodiment
The present invention will be described in further detail below with reference to the embodiments of the drawings.
As shown in Figure 1, this contains ammonium hydroxide coal slurry gasification graywater treating method includes:
Level-one evaporating column 7, including tower 71 on mutually isolated first and the first lower tower 72, the first lower tower 72 passes through the first gas
Tower 71 in the connection of phase conveyance conduit 73 first, for the steam of the first lower tower 72 to be delivered to tower on first；First gas-phase transport
The entrance of pipeline 73 is located at the top of the first lower tower, and the outlet of the first gas-phase transport pipeline 73 is located at the middle part of tower 71 on first.
The entrance of tower 71 connects buck conveyance conduit 21 on first, and buck conveyance conduit 21 is equipped with 11 He of the first feed pump
Feeder 10；Feeder 10 is located at the upstream of the first feed pump；The gas phase of the gas phase emission pipeline connection injector 3 of tower on first
Entrance；The liquid phase discharge tube of tower 71 connects tower 81 on the second of dual evaporation tower 8 by the second feed pump 12 on first.
Dual evaporation tower 8, including tower 81 on mutually isolated second and the second lower tower 82, the second lower tower 82 passes through the second gas
Tower 81 in the connection of phase conveyance conduit 83 second, for the steam of the second lower tower 81 to be delivered to tower on second；Second gas-phase transport
The entrance of pipeline 83 is located at the top of the second lower tower, and the outlet of the second gas-phase transport pipeline 83 is located at the middle part of tower 81 on second.
The gas phase entrance of the gas phase emission pipeline connection injector 3 of tower 81 on second；The liquid phase delivery pipe of tower 81 on second
Road connects the feed inlet of stripper 9 by third feed pump 13.
In the present embodiment first on tower and second tower be solid valve-type formula tower tray tower, effectively to slow down due to fouling
The mass-transfer efficiency for influencing tower tray promotes liquid phase and is uniformly mixed, and saves stripping low pressure steam consumption, finally improves whole
The efficiency of a device.
Injector 3, for controlling the pressure on first on tower and second in tower, while by tower institute on tower on first and second
The fixed gas isolated is sent into as heat source in stripper 9, to save stripped vapor；Tower and the in its first entrance connection first
The gas phase emission pipeline of tower on two, second entrance connect low-pressure steam power source, and the stripping gas of outlet connection stripper 9 enters
Mouthful.
Stripper 9, the ammonia nitrogen for being stripped off in the buck after heating, for conventional stripper, bottom sets that there are two vapour
Gas entrance is mentioned, wherein the material outlet of the first stripping gas entrance connection injector 3, the second stripping gas entrance connect low-pressure steam
Source；The liquid phase discharge tube that the material inlet of upper part passes through tower in the connection of third feed pump 13 second.
The top gas phase discharge tube of stripper 9 passes sequentially through the first air cooler 41, the first water cooler 51 connection return tank 6
Feed inlet；The material inlet of the lower tower 82 of the liquid phase discharge tube connection second of stripper.First air cooler and the first water cooler
Constitute first cooler of the present embodiment.
The material inlet that the material outlet of second lower tower 82 passes through the lower tower 72 of the 4th feed pump 14 connection first；First lower tower
72 material outlet connects buck by discharge pump 15 and discharges downstream connection qualification buck discharge tube；Edge on buck discharge tube
Buck flow direction is also successively arranged the second air cooler 42 and the second water cooler 52.Second air cooler and the second water cooler constitute this
Second cooler of embodiment.
Return tank 6, for collecting the mixture of ammonia and water vapour that stripping tower top is sent out, the material into return tank exists
This carries out gas-liquid separation, controls pressure of stripping tower using voltage-controlled valve, while reflux pump 16 being avoided to evacuate.The fixed gas isolated exists
Torch burning is sent when superpressure, and downstream sulfur recovery unit is sent to when pressure meets design objective.The liquid phase isolated is divided into two strands,
One returns to stripper from top via reflux pump 16, one extraction sends to downstream as qualified ammonium hydroxide.
The 600m generated with the gasification installation of 3,600,000 tons/year of methanol scales of coal system3/ h is illustrated for buck containing ammonia.
It is as follows that this contains ammonium hydroxide coal slurry gasification graywater treating method:
Buck after flocculation, coagulation and alkaline cleaning, removes part calcium and magnesium ion and suspended matter, while by pH tune
Section to 12 or more, it is qualified after clarification room temperature buck be forced into 0.3MPaG using the first feed pump and be delivered to tower on first, control
Tower operating pressure is -0.03MPaG on first, with the secondary flash gas from the first lower tower be directly mixed heat exchange to 70~
80 DEG C, obtain primary mixture.Then 0.4MPaG is forced into using the second feed pump be sent into tower on second, tower in control second
Operating pressure be 0.06MPaG, be directly mixed heat exchange to 100~110 DEG C with the full flashing gas from the second lower tower,
Obtain secondary mixture.Buck after heat exchange is forced into after 0.6MPaG by third feed pump to be sent to stripper.
In stripper after the low-pressure steam stripping that excess pressure is 0.4MPaG, temperature is 180 ± 5 DEG C, in stripper
Tower top obtains the rich ammonia that temperature is 130 DEG C, first passes through the first air cooler and is cooled to 60 DEG C, is cooled to using the first water cooler
Enter in return tank after 40 DEG C.
According to the reflux pump discharge of norm controlling required by product ammonium hydroxide, and send out the flow control time of out-of-bounds finished product ammonium hydroxide
Flow the liquid level of tank.It is ammonia content 15wt% that the present embodiment product ammonium hydroxide required, which sends index outside, and the reflux ratio for controlling reflux pump is
0.8.When the liquid level of return tank fluctuates, its level stability can be maintained by the uninterrupted that ammonium hydroxide is sent in control outside.
Stripper tower reactor buck after low-pressure steam strips, which is sent using pressure difference to the second lower tower, carries out full flashing, control
The operating pressure of the lower tower of system first is 0.1MPaG.Tower carries out secondary under liquid phase after flash distillation is pumped to first by the 4th charging
The operating pressure of flash distillation, the lower tower of control first is 0.05MPaG.The buck that temperature is 82 DEG C is obtained after flash distillation, is pumped by discharging
55 DEG C are first cooled to the second air cooler 11, then sends out battery limit (BL) after being cooled to 40 DEG C via the second water cooler.
The fixed gas that the temperature that tower is isolated on tower and second on first is 100 DEG C and 118 DEG C is by injector, with pressure
For 0.4MPaG, temperature is 180 ± 5 DEG C of low-pressure steams as injection power, and injection carries out recycling heat into stripper, simultaneously
As stripping gas；Finally according to the emission direction for the pressure gauge Staged cotrol device control system fixed gas being arranged on return tank 6.If
When downstream sulfur recovery processing unit failure is perhaps overhauled or when pressure exceeds scope of design, fixed gas is temporarily discharged into flare stack
Line, otherwise, fixed gas send to downstream sulfur recovery unit, improve the flexibility and safety of device independent operation.
The present embodiment and CN103964631A technique are compared.Comparison result is as shown in table 1.
Table 1
As can be seen from Table 1, steam consumption of the present invention is small, and energy-saving effect is good, and reduces equipment investment.
Claims (8)
1. a kind of graywater treating method of coal slurry gasification containing ammonium hydroxide, it is characterised in that include the following steps:
Buck after flocculant, coagulant and lye agent-feeding treatment qualification is pressurized to 0.3~0.5MPaG and is sent into tower on first
It is that the secondary flash gas that 95~105 DEG C of pressure are 0~0.1MPaG carries out Hybrid Heating with the temperature from the first lower tower, the
On one the tower bottom of tower obtain temperature be 70~80 DEG C, pressure be the logistics of -0.05~-0.02MPaG mixed once；Control described
Operating pressure on one in tower is -0.05~-0.02MPaG；
Mixed once logistics, which is forced into after 0.2~0.4MPaG, enters tower on second, with the temperature from the second lower tower be 110~
120 DEG C of pressure are that 0.15~0.2MPaG full flashing gas is mixed, and it is 100~110 that the tower bottom of tower, which obtains temperature, on second
DEG C, pressure be 0.05~0.1MPaG secondary mixture stream；Control tower on described second operating pressure be 0.05~
0.1MPaG；
Secondary mixture stream is stripped after being forced into 0.5~0.6MPaG into stripper；Stripping used in the stripper
Gas is from 0.3~0.5MPaG, 180 ± 5 DEG C of low-pressure steam and the tower on tower and described second on described first out-of-bounds
Fixed gas；The fixed gas is by injector injection to the stripper；Control the stripper operating pressure be 0.2~
0.4MPaG, temperature are 131~150 DEG C；
After stripping, the mixture of tower top the discharge ammonia and vapor of the stripper, the mixture generates not after processing
Solidifying pneumatic transmission sulfur recovery unit or torch burning, ammonium hydroxide generated are divided into two strands, wherein first strand of ammonium hydroxide returns to the stripper
Reflux operation is carried out, second strand of ammonium hydroxide is sent out out-of-bounds as ammonium hydroxide product；
The buck that the stripper tower bottom pressure is 0.3~0.4MPaG enters the second lower tower using pressure difference and carries out full flashing, control
The operating pressure for making the described second lower tower is 0.1~0.2MPaG, and the full flashing vapour generated after full flashing enters as heat source
Tower heats primary mixture on described second；
The liquid phase obtained after full flashing is pressurized to 0.1~0.3MPaG and send to the described first lower tower progress secondary flash, controls institute
The operating pressure stated in the first lower tower is 0~0.1MPaG；The gas phase generated after secondary flash enters tower on described first and is used as heat
The buck is heated in source, obtains primary mixture；
The liquid phase generated after secondary flash sends to downstream wastewater processing unit.
2. the graywater treating method of coal slurry gasification containing ammonium hydroxide according to claim 1, it is characterised in that the stripper overhead
The temperature of discharge is to enter return tank after 125~135 DEG C of gas phase is cooled to 40~45 DEG C to be cached, while isolating described
Fixed gas；The ammonium hydroxide of the generation is drawn through reflux pump, is 15% by control reflux pump flow control outlet ammonia concn
wt。
3. the graywater treating method of coal slurry gasification containing ammonium hydroxide according to claim 1, it is characterised in that the described first lower tower row
Qualified ash out sends to downstream wastewater processing unit after being water-cooled to 40~50 DEG C.
4. the graywater treating method of coal slurry gasification containing ammonium hydroxide according to any one of claims 1 to 3, it is characterised in that described
Tower and the first lower tower share the first tower body on one, and the first lower tower passes through tower in the first gas-phase transport pipeline connection first；Institute
It states the first gas-phase transport pipeline to be located at outside first tower body, the entrance of the first gas-phase transport pipeline is located at the upper of the first lower tower
Portion, the outlet of the first gas-phase transport pipeline are located at the middle part of tower on first；
Tower and the second lower tower share the second tower body on described second, and the second lower tower passes through the second gas-phase transport pipeline connection the
Tower on two；The second gas-phase transport pipeline is located at outside second tower body, and the entrance of the second gas-phase transport pipeline is located at second
The top of lower tower, the outlet of the second gas-phase transport pipeline are located at the middle part of tower on second.
5. the graywater treating method of coal slurry gasification containing ammonium hydroxide according to claim 4, it is characterised in that on described first tower and
Tower is solid valve-type tower tray tower on described second, and the quantity of tower tray is 3-5 block.
6. the graywater treating method of coal slurry gasification containing ammonium hydroxide according to claim 5, it is characterised in that on described first tower and
Pressure difference between described first lower tower is 50-100kPa；Pressure difference on described second between tower and the second lower tower is 50-
100kPa。
7. the graywater treating method of coal slurry gasification containing ammonium hydroxide according to claim 6, it is characterised in that the stripper is passed through
The amount of low-pressure steam is 8~10v% of material to be stripped.
8. the graywater treating method of coal slurry gasification containing ammonium hydroxide according to claim 7, it is characterised in that the buck to be processed
After flocculant, coagulant and lye agent-feeding treatment qualification, in i.e. normal temperature and pressure and pH value is greater than 12.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910316708.0A CN110171857A (en) | 2019-04-19 | 2019-04-19 | A kind of graywater treating method of coal slurry gasification containing ammonium hydroxide |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112107875A (en) * | 2020-10-29 | 2020-12-22 | 上海华谊工程有限公司 | Flash evaporation stripping cooling system and treatment process for black water by using same |
| CN112479291A (en) * | 2020-10-28 | 2021-03-12 | 中石化宁波工程有限公司 | Direct heat exchange black water two-stage waste heat recovery equipment and process |
| CN113526596A (en) * | 2020-04-14 | 2021-10-22 | 中科合成油工程有限公司 | Method for recycling sewage of pressurized fixed bed coal gasification process |
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|---|---|---|---|---|
| US4345975A (en) * | 1978-09-12 | 1982-08-24 | Mitsui Kensetsu Kabushiki Kaisha | Process for preventing blockage in distillation column of treatment apparatus for ammoniacal waste liquid |
| CN101306899A (en) * | 2008-05-21 | 2008-11-19 | 山西丰喜肥业（集团）股份有限公司临猗分公司 | Grey water treatment technology for graded gasification furnace |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113526596A (en) * | 2020-04-14 | 2021-10-22 | 中科合成油工程有限公司 | Method for recycling sewage of pressurized fixed bed coal gasification process |
| CN113526596B (en) * | 2020-04-14 | 2023-04-07 | 中科合成油工程有限公司 | Method for recycling sewage of pressurized fixed bed coal gasification process |
| CN112479291A (en) * | 2020-10-28 | 2021-03-12 | 中石化宁波工程有限公司 | Direct heat exchange black water two-stage waste heat recovery equipment and process |
| CN112107875A (en) * | 2020-10-29 | 2020-12-22 | 上海华谊工程有限公司 | Flash evaporation stripping cooling system and treatment process for black water by using same |
| CN112107875B (en) * | 2020-10-29 | 2023-08-15 | 上海华谊工程有限公司 | Flash evaporation steam stripping cooling system and black water treatment process using same |
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Application publication date: 20190827 |