CN102795684A - Treatment method of organic waste water of coal-to-liquids - Google Patents
Treatment method of organic waste water of coal-to-liquids Download PDFInfo
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- CN102795684A CN102795684A CN2012103125974A CN201210312597A CN102795684A CN 102795684 A CN102795684 A CN 102795684A CN 2012103125974 A CN2012103125974 A CN 2012103125974A CN 201210312597 A CN201210312597 A CN 201210312597A CN 102795684 A CN102795684 A CN 102795684A
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Abstract
The invention provides a treatment method of organic waste water of coal-to-liquids, which comprises the following steps of preheating hydrocarbonaceous gas and raw water of the organic waste water of the coal-to-liquids and then loading into a saturation tower through the lower part and the upper part of the saturation tower, conducting primary steam stripping on the organic waste water with the hydrocarbonaceous gas in the saturation tower, discharging the organic waste water subjected to the primary steam stripping from the bottom of the saturation tower, and discharging the hydrocarbonaceous gas enriched with organic matters from the top of the saturation tower; preheating water steam and the organic waste water discharged from the bottom of the saturation tower and subjected to the primary steam stripping and then loading into a stripping tower through the lower part and the upper part of the stripping tower, conducting secondary steam stripping on the organic waste water with the water steam in the stripping tower, discharging the organic waste water subjected to the secondary steam stripping from the bottom of the stripping tower, and discharging the water steam enriched with the organic matters from the top of the stripping tower. The treatment method has the advantages of short flow and simple equipment, can effectively solves the problem that the organic waste water is difficult to treat and utilize in the coal-to-liquids process, and realizes the reclamation utilization of the organic waste water.
Description
Technical field
The invention belongs to petrochemical complex comprehensive utilization field, particularly a kind of treatment process of coal system oil organic waste water.
Background technology
All the time, China is the country of " many coals few oil gas ", because growing to petroleum demand, therefore, utilizing correlation technique that coal is converted into processed oil is an important channel that solves the China's oil resource shortage.
Coal system oil (Coal-to-liquids, CTL) being is raw material with coal, a technology through chiral process is produced oil product and petrochemicals comprises two kinds of technological lines of DCL/Direct coal liquefaction and ICL for Indirect Coal Liquefaction.The direct liquefaction of coal be with coal under high-temperature and high-pressure conditions, through shortening direct liquefaction synthesizing liquid hydrocarbon fuel, and, become the oil fuel that needs through further refining (removing atoms such as sulphur, nitrogen, oxygen); Indirect coal liquefaction technology then is that synthetic gas is produced in gasification of coal, and funds-Tuo (F-T) synthesizes the production synthetic oil again, perhaps through MTG technology synthetic gasoline.
Coal system oil is produced and is realized that coal becomes in each operation of oil, can produce a large amount of waste water, and this type of waste water mainly contains organic substances such as alcohol, ketone, aldehyde, acid, ester, and composition is quite complicated, is difficult to handle through the biochemical method of routine.
At present, the ordinary method of handling this type coal system oil organic waste water has: steam stripped and steam stripped add methods such as multiple-effect evaporation concentration.For the steam stripped method, though but stripping goes out most of organism in the organic waste water, and the waste water behind the stripping still need send WWT, and the stripping thing also needs the otherwise designed outlet, and the intractability of whole processing requirement is big, and investment is high, running cost is high; And the steam stripped method of multiple-effect evaporation enrichment step is arranged for increase, and but exist energy consumption high, the waste water after the evaporation also need carry out the defective of WWT.On the other hand, present waste water treatment process only is conceived to discharge of wastewater control, also is not used effectively for the organic components in waste water resource and the waste water, still has secondary emission unavoidably and pollutes.
Along with China's constant development of economy and to the requirement of environmental protection increasingly stringent, the improvement of the three wastes has become the key subjects of Coal Chemical Industry development.When administering organic waste water, how waste water resource is realized rationally utilizing, to develop a circular economy, the resource utilization of refuse also is key subjects with utilization again.Based on above-mentioned, whether a large amount of organic waste waters that produce in the coal system oil process can be handled effectively, will affect the coal-to-oil industry development, and simultaneously, organic resource utilization also is a problem demanding prompt solution with utilization again in the waste water.
Summary of the invention
The technical problem underlying that the present invention solved provides a kind of treatment process of coal system oil organic waste water, when reducing the discharging of coal system oil organic waste water, has also realized the comprehensive utilization of waste water resource.
The present invention provides the treatment process of a kind of coal system oil organic waste water, and this treatment process comprises followingly carries out steam stripped step to said organic waste water:
The former water of gas containing hydrocarbon and coal system oil organic waste water is sent into saturator through the bottom and the top of saturator respectively through after the preheating; Realize that in saturator gas containing hydrocarbon carries out stripping No. one time to organic waste water; Discharge at the bottom of tower through the organic waste water behind the stripping, the organic gas containing hydrocarbon of enrichment is then discharged from cat head;
Organic waste water behind the stripping of discharging at the bottom of water vapor and the saturated Tata is sent into stripping tower through the bottom and the top of stripping tower respectively through after the preheating; In stripping tower, realize the secondary stripping of water vapor to organic waste water; Discharge at the bottom of tower through the organic waste water behind the secondary stripping, the organic water vapor of enrichment is then discharged from cat head.
Embodiment of the present invention; Design has also utilized mutual placed in-line saturator and stripping tower; Utilize gas containing hydrocarbon and water vapor to implement stripping twice respectively to coal system oil organic waste water, facts have proved and in the quantity discharged and concentration that significantly reduce coal system oil organic waste water, to reclaim the organism resource in the waste water; Realize the resource utilization of organic waste water, also reduced the load and the difficulty of wastewater treatment.
In embodiment of the present invention; Can be according to the character and the processing requirements of processing waste water; The waste water behind stripping and secondary stripping that saturator and stripping tower are discharged carries out the part circulation respectively, that is, and and the organic waste water at the bottom of the saturated Tata behind the stripping of discharge; A part of and former water mixes and returns saturator, and another part is sent into stripping tower and carried out the secondary stripping; Perhaps, the organic waste water behind the secondary stripping of discharging at the bottom of the stripping tower, the organic waste water behind a part of and said stripping mix and return stripping tower, and all the other are transported to follow-up water treatment operation; Also can implement the part circulation respectively, promote the steam stripped effect of waste water to the waste water of saturator and stripping tower discharge.In the concrete operations, can realize part waste water circulation on the outlet pipeline of saturator and/or stripping tower through recycle pump is set to saturator and stripping tower.
In coal chemical technology; All kinds of production processes all can produce the gas that contains carbon resource; The coal-seam gas in the coal mining for example; Coke(oven)gas that produces in the process of coking or the like, even in coal oil-producing technique process, also can give off a large amount of carbonaceous tail gas, these contain the gas of carbon resource many is staple with rudimentary hydro carbons things such as methane.At present, make raw material with this type gas (the present invention is called gas containing hydrocarbon) usually, utilize steam reforming to come preparing synthetic gas.
Steam reforming is meant hydro carbons (C
mH
n) to generate with hydrogen, carbon monoxide with water vapour be the reaction process of primary product, can represent with following formula:
C
mH
n+mH
2O→mCO+(m+n/2)H
2
Can find out that hydrocarbonaceous steam reforming meeting consumes a large amount of water vapour, with methane (CH
4) be example, revolution a part methane need to consume a part water, and in actual production process the amount ratio (H of water carbon
2O/ Σ C) then about 3, hence one can see that, and the consumption of water is far longer than the consumption of hydrocarbon compound in steam reforming process.
Proposition of the present invention is based on coal system oil treatment of Organic Wastewater technology and synthetic gas is produced technological characteristics and the problem of middle steam reforming; Utilize gas containing hydrocarbon and water vapor to carry out stripping successively to organic waste water, the waste water vaporization becomes makes gas containing hydrocarbon transform required steam, has reduced the discharging of waste water; Organism in the waste water also gets in gas containing hydrocarbon and the water vapor with gaseous form simultaneously; Common as the preparation raw material of synthetic gas, that is, when reducing discharge of wastewater, realized the utilization again of resource.Therefore; According to embodiment of the present invention, utilize gas containing hydrocarbon and water vapor stripping coal system oil organic waste water, can significantly reduce discharged waste water; The water cut of hydrocarbon-containifirst gas can improve simultaneously; Reduced the water consumption of gas containing hydrocarbon in conversion process, and the partial organic substances composition in the waste water can get into the gasification of waste water in gas containing hydrocarbon and the water vapour also, has really realized the recycling of waste water.
In the above-mentioned embodiment of the present invention, the waste water that the synthetic preparation of Fischer-Tropsch (F-T) synthetic oil process was discharged during organic waste water was produced from coal system oil.This organic waste water comprises organism such as alcohol, ketone, aldehyde, acid, ester class usually, and composition is quite complicated, is difficult to handle through the biochemical method of routine.Is example with coal through Fischer-Tropsch synthesis oil: 1 ton of processed oil of every production, produce 1.5 tons of organic waste waters approximately, and organism total contents such as alcohol wherein, ketone, aldehyde, acid, ester are about 3.5% of organic waste water.According to embodiment of the present invention, to handle this waste water being implemented in proper order the stripping of gas containing hydrocarbon and the stripping of water vapor, these organism also can be to greatest extent by recycling.So, no matter be from minimizing organism exhaust emission, still to the recycling aspect of organism resource, embodiment of the present invention all have very significant meaning.
Likewise, in the technical scheme that the present invention states on the implementation, used gas containing hydrocarbon is selected from the unstripped gas that is used to produce synthetic gas, especially can be the gas that has comprised coal system oil tail gas, coal-seam gas, coke(oven)gas, Sweet natural gas or their arbitrary combination.The major ingredient of these gases is rudimentary hydrocarbon mixtures such as methane; At first being utilized in these gas containing hydrocarbons carries out in the steam stripped process the former water of coal system oil organic waste water; Organism in the waste water is with the entering of gaseous form, also makes in the gas organic constituents by enrichment; Also be beneficial to and improve waste water vaporization effect in the secondary stripping.
According to embodiment of the present invention, the organic waste water of behind twice stripping, discharging not only total amount reduces, and organic content wherein also greatly reduces.To its water quality situation, if can reach emission standard then directly discharging, even still can not discharge, when the waste water total amount reduced, organic content also significantly reduced in the waste water, and the difficulty and the processing cost of follow-up water treatment operation also reduce.For example, can continue further to purify water and reach discharging or utilize standard again through biochemical treatment.Gas containing hydrocarbon and water vapor are behind stripping, and when having improved steam content, wherein organic components and content are increased to a certain extent, are used for transforming producing synthetic gas, not only can reduce steam consumption, also are beneficial to the yield that improves synthetic gas.
So; Embodiment of the present invention can further include; After accomplishing stripping; The organic water vapor of enrichment that the organic gas containing hydrocarbon of enrichment that the saturator cat head is discharged and stripping tower cat head are discharged collect and mix after be sent to conversion system and be used for producing of synthetic gas, will send into follow-up water treatment operation from the organic waste water behind the secondary stripping of discharge at the bottom of the stripping Tata.
In technical scheme of the present invention, before getting into stripping tower, to carry out thermal pretreatment to gas containing hydrocarbon, water vapor and organic waste water, make the feeding temperature of gas, liquid can satisfy the steam stripped needs of realization in tower.In specific embodiments; Usually the preheating temperature that makes gas containing hydrocarbon and water vapor is 300-500 ℃; The preheating temperature of sending into the organic waste water of saturator and stripping tower be 150-250 ℃ comparatively suitable; Be beneficial to and in saturator and stripping tower, utilize gas containing hydrocarbon and water vapor that organic waste water is carried out stripping, make waste water as much as possible together with organic components by stripping in gas containing hydrocarbon and water vapor.
Among the present invention program; Can be through suitable heat-exchanger rig be set; Preheating to waste water and gas utilizes the operating waste heat of treatment system, realizes effective utilization of thermal source, and concrete scheme can be; After the organic waste water behind the stripping tower secondary stripping is discharged at the bottom of the tower, be cooled, and the heat of this process of cooling is used for the preheating to the organic waste water that gets into saturator and/or stripping tower through heat-exchanger rig.For example; Pass through flow scheme design; Whether the waste water of discharging at the bottom of the stripping tower behind the secondary stripping is discharged through heat-exchanger rig is cooled after, and is heated through this heat-exchanger rig earlier from the former water of the waste water at pending water source, optionally further heat before the decision entering saturator again.This heat that produces through the interchanger heat exchange carries out thermal pretreatment to organic waste water, both can effectively utilize the heat of heat transfer process to satisfy steam stripped needs, can save the energy again, makes that resource is maximized to be utilized.
Embodiment of the present invention all do not have particular requirement for being provided with of employed saturator and stripping tower and stripping system; Promptly; Saturator and stripping tower structure, filler are selected and setting; And the selection and the setting of each stage apparatus in the multistage stripping system, all can implement according to the conventional means of chemical field and wastewater treatment industry, need not extra input and design.
For ease of statement and understanding, among the present invention, " organic waste water " waste water general designation the treatment stage of being each, " the former water of organic waste water " then refers to the organic waste water from pending waste water water source.
In sum, technical scheme of the present invention has following beneficial effect:
1, the present invention utilizes gas containing hydrocarbon and water vapor as the stripping medium organic waste water to be carried out stripping twice; Water in the waste water gets into gas containing hydrocarbon by stripping with gaseous form; Thereby reduce even or eliminated discharged waste water; The water cut of gas containing hydrocarbon is improved simultaneously, has also reduced gas containing hydrocarbon and has produced the water vapor amount that needs introducing in the synthetic gas process in conversion.
2, the present invention utilizes gas containing hydrocarbon and water vapor that organic waste water is carried out in the steam stripped process; Most of organism in the waste water can get into gas containing hydrocarbon with steam; And in the secondary stripping, water vapor enrichment once more remains in the organism in the waste water, in having reduced organic waste water organic quantity discharged with reduced concentration; Alleviated the load and the difficulty of subsequent disposal, the organism that is recovered also is converted into synthetic gas (CO+H in steam reforming process
2), realized recycling better.
3, no matter be that stripping operation or follow-up water treatment and synthetic gas are produced operation, equipments choice is not all had particular determination and requirement, therefore be beneficial to commercial application.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Fig. 2 is the process flow sheet of embodiment.
Embodiment
Through accompanying drawing and embodiment, technical scheme of the present invention is done further to describe in detail below.
With reference to shown in Figure 1, briefly shown the flow process of embodiment of the present invention.
Send into saturator from bottom and top respectively after former water (from the waste discharge of each operation of coal system oil) the heater via preheating with gas containing hydrocarbon (for example coal-seam gas, the discharging of coal system oil process tail gas, Sweet natural gas and coke(oven)gas etc.) and coal system oil organic waste water; Gas, liquid material are realized the stripping of gas containing hydrocarbon to organic waste water through counter current contact in tower; Gas containing hydrocarbon behind a stripping carries the steam of vaporization and the organic components from the waste water in the entering waste water is discharged from cat head, and the waste water of vaporization is discharged at the bottom of saturated Tata;
As shown in Figure 1; Draining can directly be pumped into stripping tower at the bottom of the tower of saturator; Also diverting valve and recycle pump can be set in pipeline; Organic waste water behind the stripping that control is discharged at the bottom of the saturated Tata, a part are recycled to mix with former water and return saturator (through the preheating of necessity), and another part is sent into stripping tower and carried out the secondary stripping.
Send into stripping tower through the bottom and the top of stripping tower respectively after the organic waste water process preheating with water vapor and behind the stripping of discharging at the bottom of coming from saturated Tata; In stripping tower, realize the secondary stripping of water vapor to organic waste water; The organic water vapor of enrichment behind the secondary stripping is discharged from cat head; Organic waste water is then discharged at the bottom of the stripping Tata; Organic waste water behind the secondary stripping of discharging at the bottom of the stripping Tata can be delivered directly to follow-up water treatment operation, also can be through diverting valve and recycle pump are set in pipeline; Make a part of waste water be recycled with a said stripping after organic waste water mix and return stripping tower, all the other are transported to follow-up water treatment operation.
Through behind above-mentioned twice stripping; The organic water vapor of enrichment that the organic gas containing hydrocarbon of enrichment that the saturator cat head is discharged and stripping tower cat head are discharged collect and mixing after be sent to conversion system and be used for producing of synthetic gas; To send into follow-up water treatment operation from the organic waste water behind the secondary stripping of discharge at the bottom of the stripping Tata, and for example send into biochemical treatment mechanism and carry out aftertreatment.
Embodiment:
With reference to shown in Figure 2, be the schema of the present invention to the practical implementation of treatment of Organic Wastewater.
Gas containing hydrocarbon, its composition (percent by volume) is CH
4: 26.98%, C
2H
6: 2.60%, H
2: 58.94%, CO:6.44%, CO
2: 0.12%, N
2: 4.67%, H
2O:0.25% is preheated to 350 ℃ of temperature through preheater 1, is that 7405kmol/h, pressure are under the condition of 2.6MPa in airshed, sends into saturator 2 from the gas inlet of bottom.
The former water of organic waste water comes from the waste water that the synthetic preparation of Fischer-Tropsch synthetic oil process is discharged, and component is following:
The former water of said organic waste water in interchanger 3 with handle after wastewater heat exchange to temperature be 123 ℃ after; At flow is that 150t/h, pressure are under the condition of 3.0MPa; The former water of this organic waste water with mix from the waste water 8 behind saturator waste water circulation line, the stripping after waste water recycle pump 7 boosts; After preheater 4 is preheated to 199 ℃, send into saturator 2 again from the liquid inlet on top.
In saturator 2; Organic waste water and gas containing hydrocarbon counter current contact realize a stripping, and the organic gas containing hydrocarbon 5 of the enrichment behind the stripping leaves from the cat head of saturator 2, and this moment, the airshed of gas containing hydrocarbon was 10804kmol/h; Temperature is 168.1 ℃, and pressure is 2.6MPa; 6 of waste water discharge pipe 6 separated into two parts after waste water recycle pump 7 boosts to 2.9MPa at the bottom of the tower: waste water 8 and waste water 9; The flow of waste water 8 is 341t/h; 168.1 ℃ of temperature, pressure 2.9MPa mixes with former water through saturator waste water circulation line; Be preheating to about 199 ℃ through preheater 4, send into saturator 2 from the liquid inlet on top and recycle.
The liquid flow rate of waste water 9 is 85.3t/h; Temperature is 168.1 ℃, and pressure 2.9MPa mixes the back with discharging at the bottom of the stripping tower and secondary stripping waste water 10 after waste water recycle pump 12 boosts and sends into stripping tower 13 from the liquid inlet on top; The gas flow of water vapor 16 is 80t/h; Temperature is 375 ℃, and pressure 2.7MPa sends into stripping tower 13 from the gas inlet of bottom.Handle initial start stage, waste water 9 is directly sent into stripping tower 13.
In stripping tower 13, organic waste water and water vapor counter current contact realize the secondary stripping, and the organic water vapor 15 of the enrichment behind the stripping leaves from the cat head of stripping tower 13, and this moment, the airshed of water vapor was 4439kmol/h, and temperature is 226 ℃, and pressure is 2.7MPa.Waste water behind the secondary stripping is discharged at the bottom of tower.
The organic gas containing hydrocarbon 5 of enrichment that saturator 2 cats head are discharged mixes (gaseous fraction of this moment is following :) with the organic water vapor 15 of enrichment that stripping tower 13 cats head are discharged, and sends into and carries out producing of synthetic gas in the conversion system;
| Component | Content (v%) | Component | Content (v%) | Component | Content (v%) |
| Methyl alcohol | 0.1137 | Methane | 13.1 | Propyl carbinol | 0.03065 |
| Ethanol | 0.23 | Caproic acid | 12ppm | Primary isoamyl alcohol | 16ppm |
| Acetaldehyde | 0.01318 | Propyl alcohol | 0.06432 | Hexanol | 44ppm |
| Acetate | 0.1405 | Isopropylformic acid | 63ppm | Enanthol | 4.2ppm |
| Acetone | 0.01152 | GBL | 11ppm | Amylalcohol | 0.01362 |
| Propionic acid | 0.01712 | ETHYLE ACETATE | 1.1ppm | Carbon monoxide | 3.13 |
| Butyraldehyde | 6.8ppm | Methyl acetate | 2.7ppm | Carbonic acid gas | 0.05549 |
| Butanone | 35ppm | Valeric acid | 34ppm | Hydrogen | 28.63 |
| Butyric acid | 64ppm | Pentanone | 8ppm | Nitrogen | 2.27 |
| Water | 50.87 | Hexanone | 3.4ppm | Ethane | 1.26 |
The organic waste water behind the secondary stripping of discharging at the bottom of the stripping tower, separated into two parts: waste water 11 and waste water 14, waste water 11 is sent into stripping tower 13 from the liquid inlet on top and is recycled after waste water recycle pump 12 is handled; Waste water 14 is sent into follow-up water treatment operation after interchanger 3 heat exchange cooling; For example biochemical treatment mechanism further handles, and certainly, confirms to reach emission standard if detect waste water 14; Then can directly discharge or utilize; This moment, the flow of waste water 14 was 85.2t/h, and temperature is 40 ℃, pressure 2.7MPa.
Above-mentioned treating processes, coal system oil organic waste water is behind twice stripping of saturator and stripping tower, and the component of organic waste water 14 is following:
Component through the oil of the coal system after gas containing hydrocarbon and twice stripping process of water vapour organic waste water can be found out; Drop to 0.0435% through various organism total contents in the organic waste water behind twice stripping by initial 3.612%, and wastewater flow rate is merely 56.8% of original bulk.
Need to prove at last; Above embodiment is only unrestricted in order to technical scheme of the present invention to be described; Although with reference to preferred embodiment the present invention has been carried out detailed explanation, those of ordinary skill in the art should be appreciated that and can make amendment or be equal to replacement technical scheme of the present invention; And not breaking away from the spirit and the scope of technical scheme of the present invention, it all should be encompassed in the middle of the claim scope of the present invention.
Claims (10)
1. the treatment process of coal system oil organic waste water is characterized in that, this treatment process comprises followingly carries out steam stripped step to said organic waste water:
The former water of gas containing hydrocarbon and coal system oil organic waste water is sent into saturator through the bottom and the top of saturator respectively through after the preheating; Realize that in saturator gas containing hydrocarbon carries out stripping No. one time to organic waste water; Discharge at the bottom of tower through the organic waste water behind the stripping, the organic gas containing hydrocarbon of enrichment is then discharged from cat head;
Organic waste water behind the stripping of discharging at the bottom of water vapor and the saturated Tata is sent into stripping tower through the bottom and the top of stripping tower respectively through after the preheating; In stripping tower, realize the secondary stripping of water vapor to organic waste water; Discharge at the bottom of tower through the organic waste water behind the secondary stripping, the organic water vapor of enrichment is then discharged from cat head.
2. treatment process according to claim 1 is characterized in that, the organic waste water behind the stripping of discharging at the bottom of the saturated Tata, a part of and former water mix and returns saturator, and another part is sent into stripping tower and carried out the secondary stripping.
3. treatment process according to claim 1 and 2 is characterized in that, the organic waste water behind the secondary stripping of discharging at the bottom of the stripping tower, the organic waste water behind a part of and said stripping mix and returns stripping tower, and all the other are transported to follow-up water treatment operation.
4. treatment process according to claim 1; It is characterized in that; Also comprise; The organic water vapor of enrichment that the organic gas containing hydrocarbon of enrichment that the saturator cat head is discharged and stripping tower cat head are discharged collect and mix after be sent to conversion system and be used for producing of synthetic gas, will send into follow-up water treatment operation from the organic waste water behind the secondary stripping of discharge at the bottom of the stripping Tata.
5. treatment process according to claim 1 is characterized in that, said coal system oil organic waste water is to prepare the waste water that the synthetic oil process is discharged from the Fischer-Tropsch synthesis procedure that coal system oil is produced.
6. treatment process according to claim 1 is characterized in that said gas containing hydrocarbon is selected from the unstripped gas that is used to produce synthetic gas.
7. treatment process according to claim 6 is characterized in that, said gas containing hydrocarbon comprises coal system oil tail gas, coal-seam gas, coke(oven)gas, Sweet natural gas or their arbitrary combination.
8. according to each described treatment process of claim 1-3, it is characterized in that the preheating temperature of said gas containing hydrocarbon and water vapor is 300-500 ℃, the preheating temperature of sending into the organic waste water of saturator and stripping tower is 150-250 ℃.
9. according to each described treatment process of claim 1-4; It is characterized in that; After the organic waste water behind the secondary stripping is discharged at the bottom of the tower, be cooled, and the heat of this process of cooling is used for the preheating to the organic waste water that gets into saturator and/or stripping tower through heat-exchanger rig.
10. treatment process according to claim 9 is characterized in that, the heat of said process of cooling is used for the preheating to the former water of the organic waste water that gets into saturator.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9222034B2 (en) | 2013-11-19 | 2015-12-29 | Uop Llc | Process for removing a product from coal tar |
| CN115990344A (en) * | 2021-10-19 | 2023-04-21 | 中国石油化工股份有限公司 | Device for removing volatile organic compounds in emulsion |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6225358B1 (en) * | 1999-02-16 | 2001-05-01 | Syntroleum Corporation | System and method for converting light hydrocarbons to heavier hydrocarbons with improved water disposal |
| WO2005113425A1 (en) * | 2004-05-20 | 2005-12-01 | The Petroleum Oil And Gas Corporation Of South Africa (Pty) Ltd. | Recovery of waste water originating from synthesis processes |
| US20080119574A1 (en) * | 2004-09-30 | 2008-05-22 | Aker Kvaerner, Inc. | Recovery of Organic Compounds Using a Saturator |
| CN101778803A (en) * | 2007-06-15 | 2010-07-14 | 艾尼股份公司 | Process for the purification of an aqueous stream coming from the fischer-tropsch reaction |
| CN101898805A (en) * | 2010-02-09 | 2010-12-01 | 神华集团有限责任公司 | Two-tower stripping treatment method for sewage in coal chemical engineering equipment |
| WO2011042806A1 (en) * | 2009-10-08 | 2011-04-14 | Eni S.P.A. | Process for the purification of an aqueous stream coming from the fischer tropsch reaction |
-
2012
- 2012-08-29 CN CN2012103125974A patent/CN102795684A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6225358B1 (en) * | 1999-02-16 | 2001-05-01 | Syntroleum Corporation | System and method for converting light hydrocarbons to heavier hydrocarbons with improved water disposal |
| WO2005113425A1 (en) * | 2004-05-20 | 2005-12-01 | The Petroleum Oil And Gas Corporation Of South Africa (Pty) Ltd. | Recovery of waste water originating from synthesis processes |
| US20080119574A1 (en) * | 2004-09-30 | 2008-05-22 | Aker Kvaerner, Inc. | Recovery of Organic Compounds Using a Saturator |
| CN101778803A (en) * | 2007-06-15 | 2010-07-14 | 艾尼股份公司 | Process for the purification of an aqueous stream coming from the fischer-tropsch reaction |
| WO2011042806A1 (en) * | 2009-10-08 | 2011-04-14 | Eni S.P.A. | Process for the purification of an aqueous stream coming from the fischer tropsch reaction |
| CN101898805A (en) * | 2010-02-09 | 2010-12-01 | 神华集团有限责任公司 | Two-tower stripping treatment method for sewage in coal chemical engineering equipment |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9222034B2 (en) | 2013-11-19 | 2015-12-29 | Uop Llc | Process for removing a product from coal tar |
| CN115990344A (en) * | 2021-10-19 | 2023-04-21 | 中国石油化工股份有限公司 | Device for removing volatile organic compounds in emulsion |
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