CN203474575U - Equipment system for coal gasification wastewater chemical engineering separation - Google Patents
Equipment system for coal gasification wastewater chemical engineering separation Download PDFInfo
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- CN203474575U CN203474575U CN201320112814.5U CN201320112814U CN203474575U CN 203474575 U CN203474575 U CN 203474575U CN 201320112814 U CN201320112814 U CN 201320112814U CN 203474575 U CN203474575 U CN 203474575U
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Abstract
The utility model discloses an equipment system for coal gasification wastewater chemical engineering separation. The equipment system consists of a deacidification and deamination tower, an extraction separation tower, a solvent steam stripping tower, a phenol recycling tower, an extracting agent storage tank, a plurality of pressure pumps, a plurality of separators, a plurality of heat exchangers and a cooler which are connected with one another through pipelines. The equipment system disclosed by the utility model ensures that quality of water subjected to chemical engineering separation meets a requirement on the quality of inlet water for subsequent biochemical treatment through a corresponding coal gasification wastewater chemical engineering separation technical process according to the physical characteristics of all types of substances in sewage and a phase equilibrium relation of a solution, and deacidification and deamination are realized in the same deacidification and deamination tower during treatment of black water, so that the PH of the sewage subjected to deacidification and deamination is effectively reduced, the phenol removal effect is enhanced, ammonia salts in the subsequent technology are reduced, the possibility of scaling and blockage of equipment is greatly reduced, and the utilization rate of the equipment is increased.
Description
Technical field
The utility model relates to coal chemical industry sewage process field, relates in particular to a kind of device systems of coal gasification waste water chemical separating.
Background technology
In coal gasification course, produce a large amount of ammonia nitrogen in high density and phenol waste water, be commonly called as " Heisui River ", at present, the method that domestic and international common employing lurgi process combines with biochemical treatment is carried out purifying treatment to " Heisui River ", to reach the emission standard that meets environmental requirement, but because phenol content in such " Heisui River " is high, pollution load is large, currently used separation method is in industrial actual moving process, the water quality of the water outlet after ubiquity is processed is difficult to reach the influent quality requirement of biochemical treatment workshop section, therefore cause processing the final discharge of water and be difficult to meet the requirement of environmental protection, and at present institute for the separating device of lurgi process employing, in the time of often can causing equipment operation due to technological reason, fouling causes situation about stopping up, had a strong impact on the normal operation of equipment operating efficiency and factory.
Utility model content
Above-mentioned defect and problem for prior art, the utility model embodiment provides and can effectively remove high ammonia nitrogen in " Heisui River ", high aldehydes matter, and the equipment that efficiently solves prior art moves the device systems of a kind of coal gasification waste water chemical separating of problem of fouling obstruction.
In order to achieve the above object, the utility model provides following technical scheme:
A device systems for coal gasification waste water chemical separating, by depickling deammoniation tower, extracting and separating tower, solvent stripping tower, phenol recovery tower, extraction agent storage tank, some pressure pumps, some separators, some interchanger, water cooler connects to form by pipeline, and water cooler is connected to depickling deammoniation tower top, and depickling deammoniation tower bottom connects interchanger A, interchanger B, interchanger B Bonding pressure pump A, pressure pump A is connected to extracting and separating tower top, extraction agent tank bottom Bonding pressure pump B, pressure pump B is connected to extracting and separating tower bottom, extracting and separating top of tower is connected to phenol recovery tower after connecting interchanger C, phenol recovery tower top is connected to extraction agent tank, phenol recovery tower bottom arranges crude phenols products export, crude phenols products export connecting pipeline phenol finished product after interchanger C is discharged, extracting and separating tower bottom is connected to solvent stripping tower after connecting interchanger D, solvent stripping tower top is connected to extraction agent tank, solvent stripping tower bottom arranges products export, depickling deammoniation tower middle part arranges material inlet, material inlet connects interchanger through interchanger A successively by pipeline, interchanger G, interchanger B, depickling deammoniation tower middle part arranges gas delivery interface, and gas delivery interface connects interchanger G successively by pipeline, separator A, interchanger E, separator B, interchanger F and separator C.
In technique scheme, described depickling deammoniation tower epimere is filler, and middle hypomere is board-like column plate, and plate number is 20-40 piece.
In technique scheme, the filler of described depickling deammoniation tower epimere is: stainless steel structured packing.
In technique scheme, the control parameter of described depickling deammoniation tower is: depickling deammoniation tower 1 pressure-controlling is at 0.4-0.7MPa, and raw material hot water inlet temperature of stabilizer is controlled at 115-140 ℃, and raw material cold water inlet temperature of stabilizer is controlled at 30-50 ℃.
In technique scheme, the control parameter of described extracting and separating tower is: extracting and separating tower 2 working pressures are normal pressure, service temperature is 50-60 ℃, extraction agent is methyl isopropyl Ketone, N-BUTYL ACETATE, diisopropyl mystery, preferably extraction agent is methyl isopropyl Ketone, and extraction agent enters in tower from extracting and separating tower bottom.
In technique scheme, the control parameter of described solvent stripping tower is: tower reactor temperature is controlled at 110-120 ℃, and tower top temperature is controlled at 90-95 ℃; Plate number is 20-40 piece.
In technique scheme, the control parameter of described phenol recovery tower is: column bottom temperature is controlled at 200-220 ℃, and tower top temperature is controlled at 110-120 ℃; Stage number is 20-40 piece.
The device systems of a kind of coal gasification waste water chemical separating that the utility model provides, according to the physical property characteristic of all kinds of materials in sewage, the phase equilibrium relationship of solution, coordinate the technical process of corresponding coal gasification waste water chemical separating, guaranteed that the water quality after chemical separating meets the influent quality requirement of follow-up biochemical treatment, while realizing " Heisui River " processing, in same depickling deammoniation tower, realize depickling and deamination, effectively reduced the PH of sewage after depickling deamination, be conducive to phenol removal effect, reduced the generation of ammonia salt in subsequent technique, reduced widely the possibility of device structure and obstruction, be conducive to improve the utilization ratio of equipment.
Accompanying drawing explanation
In order to be illustrated more clearly in the utility model embodiment or technical scheme of the prior art, to the accompanying drawing of required use in embodiment or description of the Prior Art be briefly described below, apparently, accompanying drawing in the following describes is only embodiment more of the present utility model, for those of ordinary skills, do not paying under the prerequisite of creative work, can also obtain according to these accompanying drawings other accompanying drawing.
Fig. 1 is the utility model structural representation.
Embodiment
Below in conjunction with accompanying drawing of the present utility model, the technical solution of the utility model is clearly and completely described, obviously, described embodiment is only the utility model part embodiment, rather than whole embodiment.Embodiment based in the utility model, those of ordinary skills are not making the every other embodiment obtaining under creative work prerequisite, all belong to the scope of the utility model protection.
Shown in Fig. 1, the embodiment that uses the utility model to process coal gasification waste water:
A device systems for coal gasification waste water chemical separating, comprising: depickling deammoniation tower, extracting and separating tower, solvent stripping tower, phenol recovery tower, extraction agent storage tank, some pressure pumps, some separators, some interchanger, water cooler connects to form by pipeline, and water cooler is connected to depickling deammoniation tower top, and depickling deammoniation tower bottom connects interchanger A, interchanger B, interchanger B Bonding pressure pump A, pressure pump A is connected to extracting and separating tower top, extraction agent tank bottom Bonding pressure pump B, pressure pump B is connected to extracting and separating tower bottom, extracting and separating top of tower is connected to phenol recovery tower after connecting interchanger C, phenol recovery tower top is connected to extraction agent tank, phenol recovery tower bottom arranges crude phenols products export, crude phenols products export connecting pipeline phenol finished product after interchanger C is discharged, extracting and separating tower bottom is connected to solvent stripping tower after connecting interchanger D, solvent stripping tower top is connected to extraction agent tank, solvent stripping tower bottom arranges products export, depickling deammoniation tower middle part arranges material inlet, material inlet connects interchanger through interchanger A successively by pipeline, interchanger G, interchanger B, depickling deammoniation tower middle part arranges gas delivery interface, and gas delivery interface connects interchanger G successively by pipeline, separator A, interchanger E, separator B, interchanger F and separator C.
A plurality of pressure pumps, a plurality of separator, a plurality of interchanger according to device systems processing capability requirements, selected connect according to above-mentioned position.
Described depickling deammoniation tower epimere is filler, and middle hypomere is board-like column plate, and column plate material is: stainless steel float valve, act as and carry out gas-liquid mass transfer separation.
The filler material of described depickling deammoniation tower epimere is: stainless steel structured packing, act as and carry out gas-liquid mass transfer separation.
The control parameter of described extracting and separating tower is: extracting and separating tower 2 working pressures are normal pressure, and service temperature is 55 ℃, and extraction agent is methyl isopropyl Ketone, and extraction agent enters in tower from extracting and separating tower 2 bottoms.
Former water feed rate: 30m3/h; Waste water essentially consist: total phenol 5200mg/L; NH3-N:7750mg/L; C02:4200mg/L; H2S:86mg/L; COD:25000mg/L.
Coal gasification waste water being divided into two strands and being fed into depickling deammoniation tower after pre-treatment measure such as precipitation oil removal etc., depickling deammoniation tower 1 pressure-controlling is at 0.6MPa, one material A hot water inlet temperature of stabilizer is controlled at 120 ℃, after being cooled to 40 ℃, water cooler enters from depickling deammoniation tower 1 top, one material B is heated to 110 ℃ through interchanger B, interchanger G, interchanger A and enters from depickling deammoniation tower middle part, and the alkali lye NaOH material C of 20% massfraction is from the 1 middle and lower part charging of depickling deammoniation tower.Depickling deammoniation tower 1 head temperature is 57 ℃, bottom temp is 168 ℃, the isolated sour gas of stripping is overflowed from top of tower, depickling deammoniation tower 1 middle part arranges side line and adopts ammonia, from the isolated ammonia of side line and water vapor, enter interchanger G and enter successively after separator A, interchanger E, separator B, interchanger F and separator C cooling, realize NH3 and H
20 thorough separation; Depickling deammoniation tower 1 bottom still liquid is through interchanger A, interchanger B is cooled to 45 ℃ and is pumped into extracting and separating tower 2 tops, extracting and separating tower working pressure is normal pressure, service temperature is 60 ℃, extraction agent is methyl isopropyl Ketone, from the extraction agent of extraction agent storage tank, through pressure pump B, is sent to extracting and separating tower 2 bottoms.In extracting and separating tower 2, phenol type substances in extraction agent two phase countercurrent flow extraction wastewater, the extraction phase of extracting and separating top of tower enters into phenol recovery tower 4 through interchanger C, phenol recovery tower 4 top extraction extraction agents, returning to extraction agent tank retrieval system recycles, phenol recovery tower 4 bottom extraction crude phenols products, phenol recovery tower column bottom temperature is controlled at 214 ℃, and tower top temperature is controlled at 110 ℃; Stage number is 30, crude phenols products export connecting pipeline after interchanger C, lower the temperature after phenol finished product discharge.The extracting phase of extracting and separating tower 2 bottoms enters into solvent stripping tower 3 after interchanger D, tower reactor temperature is controlled at 115 ℃, tower top temperature is controlled at 95 ℃, and the top extraction of solvent stripping tower is a small amount of extraction solvent, and solvent stripping tower 3 bottom Produced Liquids are sent to the biochemical treatment system of follow-up workshop section.Extracting and separating tower 3 head temperature are 95 ℃, and bottom temp is 120 ℃, and plate number is 30.
After above-mentioned chemical separating system operation two weeks, sampling analysis, indices is: total phenol 350mg/L; NH3-N:300mg/L; CO2 is constant; H2S is constant; COD:2000mg/L.
The above; it is only embodiment of the present utility model; but protection domain of the present utility model is not limited to this; anyly be familiar with those skilled in the art in the technical scope that the utility model discloses; can expect easily changing or replacing, within all should being encompassed in protection domain of the present utility model.Therefore, protection domain of the present utility model should be as the criterion by the described protection domain with claim.
Claims (7)
1. a device systems for coal gasification waste water chemical separating, is characterized in that: by depickling deammoniation tower, extracting and separating tower, solvent stripping tower, phenol recovery tower, extraction agent storage tank, some pressure pumps, some separators, some interchanger, water cooler connects to form by pipeline, and water cooler is connected to depickling deammoniation tower top, and depickling deammoniation tower bottom connects interchanger A, interchanger B, interchanger B Bonding pressure pump A, pressure pump A is connected to extracting and separating tower top, extraction agent tank bottom Bonding pressure pump B, pressure pump B is connected to extracting and separating tower bottom, extracting and separating top of tower is connected to phenol recovery tower after connecting interchanger C, phenol recovery tower top is connected to extraction agent tank, phenol recovery tower bottom arranges crude phenols products export, crude phenols products export connecting pipeline phenol finished product after interchanger C is discharged, extracting and separating tower bottom is connected to solvent stripping tower after connecting interchanger D, solvent stripping tower top is connected to extraction agent tank, solvent stripping tower bottom arranges products export, depickling deammoniation tower middle part arranges material inlet, material inlet connects interchanger through interchanger A successively by pipeline, interchanger G, interchanger B, depickling deammoniation tower middle part arranges gas delivery interface, and gas delivery interface connects interchanger G successively by pipeline, separator A, interchanger E, separator B, interchanger F and separator C.
2. the device systems of a kind of coal gasification waste water chemical separating according to claim 1, is characterized in that: described depickling deammoniation tower epimere is filler, and middle hypomere is board-like column plate, and plate number is 20-40 piece.
3. the device systems of a kind of coal gasification waste water chemical separating according to claim 2, is characterized in that: the filler of described depickling deammoniation tower epimere is: stainless steel structured packing.
4. the device systems of a kind of coal gasification waste water chemical separating according to claim 1 and 2, it is characterized in that: the control parameter of described depickling deammoniation tower is: depickling deammoniation tower pressure-controlling is at 0.4-0.7MPa, raw material hot water inlet temperature of stabilizer is controlled at 115-140 ℃, and raw material cold water inlet temperature of stabilizer is controlled at 30-50 ℃.
5. according to the device systems of a kind of coal gasification waste water chemical separating described in claim l or 2, it is characterized in that: the control parameter of described extracting and separating tower is: extracting and separating tower working pressure is normal pressure, service temperature is 50-60 ℃, extraction agent is methyl isopropyl Ketone, and extraction agent enters in tower from extracting and separating tower bottom.
6. the device systems of a kind of coal gasification waste water chemical separating according to claim 1 and 2, is characterized in that: the control parameter of described solvent stripping tower is: tower reactor temperature is controlled at 110-120 ℃, and tower top temperature is controlled at 90-95 ℃; Plate number is 20-40 piece.
7. the device systems of a kind of coal gasification waste water chemical separating according to claim 4, is characterized in that: the control parameter of described phenol recovery tower is: column bottom temperature is controlled at 200-220 ℃, and tower top temperature is controlled at 110-120 ℃; Stage number is 20-40 piece.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320112814.5U CN203474575U (en) | 2013-03-13 | 2013-03-13 | Equipment system for coal gasification wastewater chemical engineering separation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320112814.5U CN203474575U (en) | 2013-03-13 | 2013-03-13 | Equipment system for coal gasification wastewater chemical engineering separation |
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| CN203474575U true CN203474575U (en) | 2014-03-12 |
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| CN201320112814.5U Expired - Fee Related CN203474575U (en) | 2013-03-13 | 2013-03-13 | Equipment system for coal gasification wastewater chemical engineering separation |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104829032A (en) * | 2015-05-20 | 2015-08-12 | 武汉宏澳绿色能源工程有限责任公司 | Ammonia-nitrogen wastewater treatment system |
| CN109381887A (en) * | 2017-08-03 | 2019-02-26 | 中国石油化工股份有限公司 | The pretreatment system and method for the high ammonia nitrogen acidity condensate liquid of converter unit |
| CN111592168A (en) * | 2020-06-30 | 2020-08-28 | 查都（上海）科技有限公司 | Phenol ammonia recovery unit of long period operation |
-
2013
- 2013-03-13 CN CN201320112814.5U patent/CN203474575U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104829032A (en) * | 2015-05-20 | 2015-08-12 | 武汉宏澳绿色能源工程有限责任公司 | Ammonia-nitrogen wastewater treatment system |
| CN109381887A (en) * | 2017-08-03 | 2019-02-26 | 中国石油化工股份有限公司 | The pretreatment system and method for the high ammonia nitrogen acidity condensate liquid of converter unit |
| CN111592168A (en) * | 2020-06-30 | 2020-08-28 | 查都（上海）科技有限公司 | Phenol ammonia recovery unit of long period operation |
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Granted publication date: 20140312 Termination date: 20210313 |