CN105174675A - Treatment method for coal-gasification wastewater biochemical sludge - Google Patents
Treatment method for coal-gasification wastewater biochemical sludge Download PDFInfo
- Publication number
- CN105174675A CN105174675A CN201510542316.8A CN201510542316A CN105174675A CN 105174675 A CN105174675 A CN 105174675A CN 201510542316 A CN201510542316 A CN 201510542316A CN 105174675 A CN105174675 A CN 105174675A
- Authority
- CN
- China
- Prior art keywords
- oxygen
- biochemical sludge
- gas
- liquid
- coal gasification
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Treatment Of Sludge (AREA)
Abstract
The invention provides a treatment method for coal-gasification wastewater biochemical sludge. The method comprises the following steps: 1) transporting the coal-gasification wastewater biochemical sludge into a heating furnace and carrying out preheating; meanwhile, transporting liquid oxygen into a condenser and carrying out heat exchanging and then carrying out transporting into an oxygen buffer tank; 2) respectively allowing the preheated coal-gasification wastewater biochemical sludge and an oxidant from the oxygen buffer tank to enter a supercritical water oxidation reactor, and carrying out oxidation reaction; 3) cooling the oxidized high-temperature fluid via a heat exchanger and then carrying out transporting to a high-pressure gas-liquid separator; 4) discharging a separated liquid-phase product from the bottom part of the high-pressure gas-liquid separator, and transporting a gas-phase product to a dehydrating tower from the top part of the high-pressure gas-liquid separator; 5) cooling the dehydrated gas-phase product through heat exchanging of the condenser, and carrying out transporting to a CO2 purification tower; and 6) discharging the separated liquid-phase CO2 from the bottom part of the CO2 purification tower, and transporting the oxygen in the gas-phase product back to the oxygen buffer tank from the top part of the CO2 purification tower, wherein the oxygen is circularly used as the oxidant. The treatment method for the coal-gasification wastewater biochemical sludge provided by the invention realizes rapid and thorough degradation of organic matters in the coal-gasification wastewater biochemical sludge; meanwhile, cyclic utilization of the oxygen and recovery of the CO2 in the treatment process are realized, so energy is maximumly utilized.
Description
Technical field
The present invention relates to the treatment process that a kind of organic waste are innoxious, particularly about a kind for the treatment of process of coal gasification waste water biochemical sludge.
Background technology
Coal gasification waste water biochemical sludge refers to the mud that the waste water produced in coal gasification course produces in biochemical treatment process.The wastewater flow rate produced in coal gasification course is very huge, to produce 3000000000 Nm per year
3the coal gasification plant of Sweet natural gas is example, and the coal gasification waste water of discharge is about 600t/h.According to statistics, domestic at present have nearly 10 coal gasification plants what run, and annual capacity summation is about 20,000,000,000 Nm
3, waste water annual emissions reaches 4,280 ten thousand tons.The core methed of current coal gasification waste water process adopts biochemical treatment process, but the method often processes 1000 tons of waste water will have the generation of 3 ~ 4 tons of mud.And containing hazardous and noxious substances such as a large amount of phenol, polycyclic aromatic hydrocarbons, heavy metals in coal gasification waste water biochemical sludge, if processed not in time, high risks can be caused to environment.But chemical enterprise is the method adopting burning, landfill or entrust process for the process of this kind of mud mostly, and not only the feature of environmental protection is poor but also cost is higher for these methods.In order to address this problem, there is the way utilizing supercritical Water Oxidation Technology to process mud in recent years.Supercritical Water Oxidation Technology is the chemical property utilizing water unique at supercritical conditions, i.e. temperature T>374.15 DEG C, under pressure P>22.12MPa state, after adding excess of oxygen, there is oxidizing reaction in organism, be converted into the objectionable impurities in mud with CO under supercritical water homogeneous phase condition
2, H
2o is main product.But in actual motion, for improving organic removal rate, usually need add excessive oxygenant, but because oxygenant can not recycle, therefore need continuous supplemental oxidant in oxidation reaction process, this makes oxidant consumption amount very big, causes system lignin-sludge cost to increase.
Summary of the invention
For the problems referred to above, the object of this invention is to provide a kind for the treatment of process realizing the coal gasification waste water biochemical sludge that Recycling of oxidize uses.
For achieving the above object, the present invention takes following technical scheme: a kind for the treatment of process of coal gasification waste water biochemical sludge, and it comprises the following steps:
1) by coal gasification waste water biochemical sludge by carrying out preheating in pump delivery to process furnace; Meanwhile, by liquid oxygen by heat exchange in pump delivery to condenser, then the liquid oxygen after heat exchange is transported in oxygen surge tank cushions, use as oxygenant;
2) the coal gasification waste water biochemical sludge after process furnace preheating is transported in overcritical water oxidization reactor; Be transported in overcritical water oxidization reactor by the oxygenant after peroxide surge tank buffering, oxygenant and coal gasification waste water biochemical sludge carry out oxidizing reaction in overcritical water oxidization reactor simultaneously;
3) by the high temperature fluid after overcritical water oxidization reactor oxidation after interchanger heat exchange, then be transported in high-pressure gas-liquid separator and carry out gas-liquid separation;
4) discharged the bottom of the liquid product after high-pressure gas-liquid separator is separated by high-pressure gas-liquid separator, gas-phase product is transported in dehydration tower by the top of high-pressure gas-liquid separator and carries out processed;
5) gas-phase product after the filler dehydration of dehydration tower is transported in condenser with after liquid oxygen heat exchange and is transported to CO
2in purification tower;
6) through CO
2liquid phase CO after purification tower is separated
2by CO
2discharge bottom purification tower and reclaim, the oxygen in gas-phase product is through CO
2purification tower top returns in oxygen surge tank and uses as Recycling of oxidize;
7) when after system stable operation, can process furnace be closed, coal gasification waste water biochemical sludge is delivered directly to heat exchange in interchanger through pump, then be transported in overcritical water oxidization reactor and carry out oxidizing reaction with the oxygenant from oxygen surge tank.
The filler of dehydration tower adopts molecular sieve or silica gel material.
Gas-phase product is by the CO that liquefies after condenser condenses
2temperature be-10 ~-20 DEG C, the temperature of liquid oxygen is 0 ~ 30 DEG C.
Coal gasification waste water biochemical sludge is 300 ~ 550 DEG C by temperature after interchanger heat exchange, and pressure is 22 ~ 32MPa.
The present invention is owing to taking above technical scheme, and it has the following advantages: 1, the inventive method achieves organic thorough degraded in coal gasification waste water biochemical sludge, makes fluid qualified discharge after process.2, adopt high power coefficient of oxidation amount realize organic rapidly and efficiently remove while, and combined process feature makes full use of the cold energy of liquid oxygen in system, achieves recycle and the CO of oxygen
2recovery, internal system energy is maximized the use.3, the inventive method is simple to operate, and oxidant consumption amount is little, effectively controls the cost of system lignin-sludge.
Accompanying drawing explanation
Fig. 1 is overall flow schematic diagram of the present invention.
Embodiment
Below in conjunction with drawings and Examples, the present invention is described in detail.
As shown in Figure 1, the treatment process of coal gasification waste water biochemical sludge of the present invention comprises the following steps:
1) coal gasification waste water biochemical sludge is transported in process furnace 2 by pump 1 carries out preheating; Meanwhile, liquid oxygen is transported to heat exchange in condenser 9 by pump 5, then the liquid oxygen after heat exchange is transported in oxygen surge tank 6 cushions, use as oxygenant;
2) the coal gasification waste water biochemical sludge after process furnace 2 preheating is transported to overcritical water oxidization reactor 3; Oxygenant after cushioning through peroxide surge tank 6 is transported to overcritical water oxidization reactor 3, oxygenant and coal gasification waste water biochemical sludge carry out oxidizing reaction in overcritical water oxidization reactor 3 simultaneously;
3) by after the elevated temperature fluid conveyance after overcritical water oxidization reactor 3 is oxidized to interchanger 4 heat exchange, then be transported in high-pressure gas-liquid separator 7 and carry out gas-liquid separation;
4) discharged the bottom of the liquid product after high-pressure gas-liquid separator 7 is separated by high-pressure gas-liquid separator 7, gas-phase product is transported in dehydration tower 8 by the top of high-pressure gas-liquid separator 7 and carries out processed;
5) gas-phase product after the filler dehydration of dehydration tower 8 is transported in condenser 9 with after liquid oxygen heat exchange and is delivered to CO
2purification tower 10;
6) will through CO
2liquid phase CO after purification tower 10 is separated
2by CO
2discharge bottom purification tower 10 and reclaim, the oxygen in gas-phase product is through CO
2purification tower 10 top returns in oxygen surge tank 6 and uses as Recycling of oxidize;
7) when after system stable operation, process furnace 2 can be closed, coal gasification waste water biochemical sludge is delivered directly to heat exchange in interchanger 4 through pump 1, then the oxygenant be transported in overcritical water oxidization reactor 3 and from oxygen surge tank 6 carries out oxidizing reaction.
In above-described embodiment, coal gasification waste water biochemical sludge is 300 ~ 550 DEG C by temperature after interchanger 4 heat exchange, and pressure is 22 ~ 32MPa.
In above-described embodiment, the filler of dehydration tower 8 can adopt molecular sieve or silica gel material.
In above-described embodiment, the gas-phase product after dehydration tower 8 dewaters is by after condenser 9 condensation, and liquefy CO
2temperature be-10 ~-20 DEG C, the temperature of liquid oxygen is 0 ~ 30 DEG C, again gasifies to liquid oxygen without the need to air gasification device.
In above-described embodiment, CO
2the filler of purification tower 10 can use structured packing or dumped packing.
Below by specific embodiment, in order to technique effect of the present invention to be described.
Embodiment 1
Be 100t/d to treatment capacity, water ratio be 80%, chemical oxygen demand (COD) 180000mg/L coal gasification waste water biochemical sludge process.
First coal gasification waste water biochemical sludge is transported in process furnace 2 by pump 1 and is preheated to 410 DEG C, then enter overcritical water oxidization reactor 3; Be that the liquid oxygen of sludge chemical oxygen requirement amount 3 times is transported to heat exchange in condenser 9 through pump 5 by mass rate, oxygen is gasificated into after liquid oxygen heat absorption, enter overcritical water oxidization reactor 3 through oxygen surge tank 6, there is oxidizing reaction with the coal gasification waste water biochemical sludge from process furnace 2 in oxygen in overcritical water oxidization reactor 3; Then the fluid being 600 DEG C by temperature after reaction is transported in interchanger 4 and carries out heat exchange, and it is 45 DEG C that the fluid after heat exchange is transported to temperature, carries out gas-liquid separation in the high-pressure gas-liquid separator 7 of pressure 25MPa; Liquid product after high-pressure gas-liquid separator 7 is separated is discharged by the bottom of high-pressure gas-liquid separator 7, and gas-phase product is transported in dehydration tower 8 by the top of high-pressure gas-liquid separator 7 and carries out processed; By the gas-phase product after dewatering through dehydration tower 8 and the liquid oxygen heat exchange in condenser 9 to-20 DEG C, the CO in gas-phase product
2be condensed into liquid, then by liquid phase CO
2be transported to CO
2in purification tower 10; Through CO
2purification tower 10 is separated the liquid phase CO that rear purity reaches 99%
2by CO
2discharge bottom purification tower 10 and reclaim, the oxygen in gas-phase product is through CO
2purification tower 10 top returns in oxygen surge tank 6 and uses as Recycling of oxidize.
When after system stable operation, process furnace 2 can be closed, coal gasification waste water biochemical sludge is delivered directly in interchanger 4 through pump 1 and absorb heat, be then transported in overcritical water oxidization reactor 3 and carry out oxidizing reaction with the oxygenant from oxygen surge tank 6.In this embodiment, after the process of coal gasification waste water biochemical sludge, the chemical oxygen demand (COD) of water outlet is 58mg/L, reaches national GB8978-1996 first discharge standard.
The various embodiments described above are only for illustration of the present invention, and wherein the structure, mode of connection etc. of each parts all can change to some extent, and every equivalents of carrying out on the basis of technical solution of the present invention and improvement, all should not get rid of outside protection scope of the present invention.
Claims (4)
1. a treatment process for coal gasification waste water biochemical sludge, it comprises the following steps:
1) by coal gasification waste water biochemical sludge by carrying out preheating in pump delivery to process furnace; Meanwhile, by liquid oxygen by heat exchange in pump delivery to condenser, then the liquid oxygen after heat exchange is transported in oxygen surge tank cushions, use as oxygenant;
2) the coal gasification waste water biochemical sludge after process furnace preheating is transported in overcritical water oxidization reactor; Be transported in overcritical water oxidization reactor by the oxygenant after peroxide surge tank buffering, oxygenant and coal gasification waste water biochemical sludge carry out oxidizing reaction in overcritical water oxidization reactor simultaneously;
3) by the high temperature fluid after overcritical water oxidization reactor oxidation after interchanger heat exchange, then be transported in high-pressure gas-liquid separator and carry out gas-liquid separation;
4) discharged the bottom of the liquid product after high-pressure gas-liquid separator is separated by high-pressure gas-liquid separator, gas-phase product is transported in dehydration tower by the top of high-pressure gas-liquid separator and carries out processed;
5) gas-phase product after the filler dehydration of dehydration tower is transported in condenser with after liquid oxygen heat exchange and is transported to CO
2in purification tower;
6) through CO
2liquid phase CO after purification tower is separated
2by CO
2discharge bottom purification tower and reclaim, the oxygen in gas-phase product is through CO
2purification tower top returns in oxygen surge tank and uses as Recycling of oxidize;
7) when after system stable operation, can process furnace be closed, coal gasification waste water biochemical sludge is delivered directly to heat exchange in interchanger through pump, then be transported in overcritical water oxidization reactor and carry out oxidizing reaction with the oxygenant from oxygen surge tank.
2. the treatment process of a kind of coal gasification waste water biochemical sludge as claimed in claim 1, is characterized in that: the filler of dehydration tower adopts molecular sieve or silica gel material.
3. the treatment process of a kind of coal gasification waste water biochemical sludge as claimed in claim 1, is characterized in that: gas-phase product is by the CO that liquefies after condenser condenses
2temperature be-10 ~-20 DEG C, the temperature of liquid oxygen is 0 ~ 30 DEG C.
4. the treatment process of a kind of coal gasification waste water biochemical sludge as claimed in claim 1, it is characterized in that: coal gasification waste water biochemical sludge is 300 ~ 550 DEG C by temperature after interchanger heat exchange, pressure is 22 ~ 32MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510542316.8A CN105174675A (en) | 2015-08-28 | 2015-08-28 | Treatment method for coal-gasification wastewater biochemical sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510542316.8A CN105174675A (en) | 2015-08-28 | 2015-08-28 | Treatment method for coal-gasification wastewater biochemical sludge |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105174675A true CN105174675A (en) | 2015-12-23 |
Family
ID=54897214
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510542316.8A Pending CN105174675A (en) | 2015-08-28 | 2015-08-28 | Treatment method for coal-gasification wastewater biochemical sludge |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105174675A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105676764A (en) * | 2016-02-03 | 2016-06-15 | 总装备部工程设计研究总院 | Safety monitoring system for supercritical water oxidation apparatus |
| CN106986358A (en) * | 2017-04-13 | 2017-07-28 | 安徽广信农化股份有限公司 | A kind of purifying technique of pyraclostrobin by-product sodium sulphate |
| CN108913209A (en) * | 2018-09-30 | 2018-11-30 | 重庆赛迪热工环保工程技术有限公司 | A kind of multi-joint journey recycling treatment difficulty of supercritical water decomposes the method and system of organic hazardous waste |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002273494A (en) * | 2001-03-14 | 2002-09-24 | Mitsubishi Heavy Ind Ltd | Method of treating organic solid containing inorganic salt, particularly sewer sludge |
| CN101544419A (en) * | 2008-03-27 | 2009-09-30 | 楼龙春 | Method and device for oxidizing and treating sewage or sludge containing organic substances by supercritical water |
| CN101607772A (en) * | 2009-05-05 | 2009-12-23 | 西安交通大学 | The supercritical water treatment of waste organic matter and recycling system |
| CN101698517A (en) * | 2009-11-03 | 2010-04-28 | 西安交通大学 | Supercritical water treatment system with blockage clearing function and blockage clearing method thereof |
| CN102477312A (en) * | 2010-11-29 | 2012-05-30 | 新奥科技发展有限公司 | Method for gasifying carbon-containing substance by using supercritical water |
| CN102503066A (en) * | 2011-12-23 | 2012-06-20 | 南京工业大学 | System and method for supercritical water oxidation treatment and resource utilization of organic sludge |
| CN102642947A (en) * | 2012-04-23 | 2012-08-22 | 西安交通大学 | Supercritical water oxidization treatment system for high-salinity organic waste water |
| CN104326637A (en) * | 2014-10-21 | 2015-02-04 | 新奥科技发展有限公司 | Sludge treatment method |
| CN204569599U (en) * | 2015-01-19 | 2015-08-19 | 王冰 | A kind of novel no pollution sewage effluent total system |
-
2015
- 2015-08-28 CN CN201510542316.8A patent/CN105174675A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002273494A (en) * | 2001-03-14 | 2002-09-24 | Mitsubishi Heavy Ind Ltd | Method of treating organic solid containing inorganic salt, particularly sewer sludge |
| CN101544419A (en) * | 2008-03-27 | 2009-09-30 | 楼龙春 | Method and device for oxidizing and treating sewage or sludge containing organic substances by supercritical water |
| CN101607772A (en) * | 2009-05-05 | 2009-12-23 | 西安交通大学 | The supercritical water treatment of waste organic matter and recycling system |
| CN101698517A (en) * | 2009-11-03 | 2010-04-28 | 西安交通大学 | Supercritical water treatment system with blockage clearing function and blockage clearing method thereof |
| CN102477312A (en) * | 2010-11-29 | 2012-05-30 | 新奥科技发展有限公司 | Method for gasifying carbon-containing substance by using supercritical water |
| CN102503066A (en) * | 2011-12-23 | 2012-06-20 | 南京工业大学 | System and method for supercritical water oxidation treatment and resource utilization of organic sludge |
| CN102642947A (en) * | 2012-04-23 | 2012-08-22 | 西安交通大学 | Supercritical water oxidization treatment system for high-salinity organic waste water |
| CN104326637A (en) * | 2014-10-21 | 2015-02-04 | 新奥科技发展有限公司 | Sludge treatment method |
| CN204569599U (en) * | 2015-01-19 | 2015-08-19 | 王冰 | A kind of novel no pollution sewage effluent total system |
Non-Patent Citations (3)
| Title |
|---|
| 中国环境科学学会: "《中国环境科学学会学术年会论文集（2010）第三卷》", 31 December 2010, 中国环境科学出版社 * |
| 于广欣等: "煤气化废水的超临界水氧化处理实验", 《工业水处理》 * |
| 郭揆常: "《液化天然气（LNG）工艺与工程》", 31 May 2014, 中国石化出版社 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105676764A (en) * | 2016-02-03 | 2016-06-15 | 总装备部工程设计研究总院 | Safety monitoring system for supercritical water oxidation apparatus |
| CN106986358A (en) * | 2017-04-13 | 2017-07-28 | 安徽广信农化股份有限公司 | A kind of purifying technique of pyraclostrobin by-product sodium sulphate |
| CN108913209A (en) * | 2018-09-30 | 2018-11-30 | 重庆赛迪热工环保工程技术有限公司 | A kind of multi-joint journey recycling treatment difficulty of supercritical water decomposes the method and system of organic hazardous waste |
| CN108913209B (en) * | 2018-09-30 | 2023-11-03 | 重庆赛迪热工环保工程技术有限公司 | Method and system for supercritical water multi-pass resource treatment of recalcitrant organic hazardous waste |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102874916B (en) | Supercritical water gasification-oxidation method for treating organic wastewater and recycling synthesis gas | |
| CN104560201B (en) | The production technology and system and ammonia synthesis process and system of high-purity hydrogen | |
| CN110054164B (en) | Concentrated recovery system of dilute sulfuric acid | |
| CN107413164B (en) | Process and device for recycling and treating organic waste gas by secondary membrane | |
| CN102633350B (en) | Method for recycling excessive oxygen and carbon dioxide in supercritical water oxidation system | |
| CN104843813A (en) | Coal gasification high ammonia nitrogen wastewater treatment process | |
| CN105174675A (en) | Treatment method for coal-gasification wastewater biochemical sludge | |
| CN113560319B (en) | Solvent gasification pyrolysis device and method for waste circuit board | |
| CN106698785A (en) | Coal gasification wastewater phenol and ammonia recovery process | |
| CN109370641B (en) | Efficient heavy oil treatment system and process | |
| Nurjanah et al. | Energy saving in NMP (N-methyl-2-pyrrolidone) recovery process by numerical modeling | |
| CN201158601Y (en) | System for treating carbonized wastewater or organic waste water with supercritical water oxidization technique | |
| CN209771738U (en) | Liquid nitrogen low-temperature condensation VOC recovery processing device | |
| CN111692838A (en) | Rare gas krypton-xenon refining and ultrapure oxygen production device and production process | |
| CN111234873A (en) | Supercritical water gasification system and method with energy recovery and zero wastewater discharge | |
| CN108585165B (en) | Ammonia recovery system for supercritical water oxidation system and ammonia recovery control method | |
| CN216629750U (en) | System for separate pentaerythritol and calcium formate from pentaerythritol mother liquor | |
| CN101265153A (en) | Technique for reclaiming organic hydrocarbon and nitrogen gas from polyethylene device tail gas | |
| CN103616858B (en) | The oxygen recovery control system of the difficult biochemical nitrogenous dense organic wastewater of SCWO process and method | |
| CN115849301A (en) | Hydrogen production device and method based on hydrogen storage by formic acid | |
| CN204111354U (en) | A kind of sour water steam stripping at reduced pressure device | |
| CN102500193B (en) | Recovery and utilization method for tail gas in DMF (Dimethyfumarate) synthetic tower and device | |
| EP2563498B1 (en) | Biogas upgrading | |
| CN206385087U (en) | A kind of device of the single benzene ring type compounds of biomass pyrolytic volatile matter hydrogenation refining | |
| CN202446969U (en) | Water cooling type variable pressure waste gas absorption recycling device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20151223 |