CN203079784U - Deamination oil-removing device - Google Patents
Deamination oil-removing device Download PDFInfo
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- CN203079784U CN203079784U CN 201220727012 CN201220727012U CN203079784U CN 203079784 U CN203079784 U CN 203079784U CN 201220727012 CN201220727012 CN 201220727012 CN 201220727012 U CN201220727012 U CN 201220727012U CN 203079784 U CN203079784 U CN 203079784U
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- deamination
- oil
- lime set
- ammonia
- water
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Abstract
The utility model provides a deamination oil-removing device. The deamination oil-removing device comprises a deamination tower 1, as well as a primary condenser 2, a primary liquid separating tank 3, a secondary condensing cooler 4, a secondary liquid separating tank 5, a tertiary condensing condenser 6 and a tertiary liquid separating tank 7 which are connected with the tower top of the deamination tower 1 in sequence, wherein the lower parts of the primary liquid separating tank 3, the secondary liquid separating tank 5 and the tertiary liquid separating tank 7 are connected with an ammonia condensate oil separating tank 8; a de-acidified phenolated water input port 9 is formed in the upper part of the deamination tower 1; a deamination water output port 10 is formed in the lower part of the deamination tower 1; and an ammonia gas output port 11 is formed in the upper part of the tertiary liquid separating tank. The deamination oil-removing device is simpler in structure, clear in process, convenient to operate and good in oil-removing effect.
Description
Technical field
The utility model relates to a kind of oil removal plant, is specifically related to a kind of deamination oil removal plant that is used to handle coal gasification waste water.
Background technology
Coal gasification waste water still contains oil after carrying out oil removing, dedusting through the gas liquor tripping device in the phenol water.Simultaneously, phenol ammonia reclaiming process in the past can not be removed these oil.This just causes extraction wherein that emulsification partly takes place easily, and makes the column plate of deammoniation tower and extraction tower fouling and latch up phenomenon occur, has shortened the cycle of operation of device, is unfavorable for enhancing productivity.In addition, if oil enters biochemical treatment workshop section, also can have a strong impact on the normal operation of biochemical treatment system.
Therefore, also need a kind of simple in structure, easy to operate oil removal plant at present, to remove the oil in the phenol water.
The utility model content
Therefore, the purpose of this utility model is to overcome defective of the prior art and blank, and a kind of deamination oil removal plant is provided, this apparatus structure is simple, technology is clear, easy to operate, can remove the oil in the phenol water effectively, simultaneously can also ammonia gas as byproduct and light oil, have higher promotional value.
The utility model provides a kind of deamination oil removal plant, described device comprises that deammoniation tower 1, the one-level condensate cooler 2, the one-level that are connected with the cat head of described deammoniation tower 1 preface successively divide flow container 3, B-grade condensation water cooler 4, secondary to divide flow container 5, three grades of condensate coolers 6 and three fraction flow containers 7, the bottom that described one-level divides flow container 3, secondary to divide flow container 5 and three fraction flow containers 7 all divides oil tank 8 to be connected with the ammonia lime set, the top of described deammoniation tower 1 is provided with depickling phenol water input 9, and the bottom is provided with deamination water output 10; The top of described three fraction flow containers is provided with ammonia delivery port 11.
The utility model creatively with deamination device and oil removal plant combination in addition, just can effectively be removed the oil in the phenol water in the deamination process.And isolating ammonia lime set is divided in the oil tank 8 in the ammonia lime set and is compiled in the condenser.Because the oil concentration in the ammonia lime set is higher, is easier to standing demix, can obtain byproduct light oil after the separation.
The contriver is surprised to find that also three grades of condensation separation that the utility model adopted are best to the oil separating effect.As be less than three grades and then can not reach the ideal effect, make the ammonia content in the phenol water defective; As more than three grades, then can cause the raising of apparatus cost and unnecessary expense expenditure, and not obvious to the lifting of separating effect.
The depickling phenol water input 9 of described deammoniation tower is used to import the phenol water of handling through depickling.Those skilled in the art all knows, and the depickling of phenol water is handled and typically referred to the CO that removes in the phenol water
2And H
2Acidic impurities such as S.
According to device of the present utility model, wherein, described deammoniation tower 1 can also be connected with deammoniation tower reboiler 12.Described deammoniation tower can use deammoniation tower reboiler 12, adopts 1.0MPa(g), 184 ℃ steam heats, and volatile matter such as ammonia is put forward by gas.As preferably, the temperature of deammoniation tower cat head is controlled at 125 ~ 140 ℃, tower top pressure is controlled at 0.3 ~ 0.4MPa, tower still temperature is controlled at 150 ~ 160 ℃, and tower still pressure-controlling is at 0.35 ~ 0.45MPa, under this condition, ammonia in the phenol water, oil gas, water vapour and some other easy volatile material all can be carried by gas, through condensation and vacuum flashing, purify ammonia, separate out oil phase at last.
According to device of the present utility model, wherein, described one-level divides flow container 3 and secondary to divide flow container 5 and described ammonia lime set to divide also can be connected with ammonia lime set water cooler 13 between the oil tank 8.One-level divides liquid phase that flow container and secondary divide the flow container bottom after the cooling of ammonia lime set water cooler, can together enter the ammonia lime set with the liquid phase of the bottom of three fraction flow containers and divide oil tank.As preferably, the thick ammonia of the cat head output of deammoniation tower is after 2 heat exchange of one-level condensate cooler are cooled to about 125 ~ 140 ℃, enter one-level and divide flow container 3, carry out gas-liquid separation, gas phase enters B-grade condensation water cooler 4 after the output of top, enter secondary after heat exchange is cooled to about 70 ~ 90 ℃ and divide flow container 5, gas phase is from the top extraction, enters three fraction flow containers 7 after about three grades of condensate cooler 6 heat exchange to 50 ℃.Like this, the wet goods impurity in the thick ammonia of three grades of condensation process is removed, from ammonia delivery port 11 exportable comparatively purified ammonias.
According to device of the present utility model, wherein, described ammonia lime set divides oil tank 8 to be connected with ammonia lime set pump 14, and described ammonia lime set pump 14 can be connected with gas liquor basin 15 with the top of described deammoniation tower 1 respectively.The ammonia lime set is divided in the oil tank after the water after the oil removing is boosted by ammonia lime set pump 14, and a part can be used as the trim the top of column phase of deammoniation tower, and another part can loop back the gas liquor basin of gas liquor product separation.
According to device of the present utility model, wherein, described ammonia lime set pump 14 only is connected with the top of described deammoniation tower 1.Because the aqueous phase oleaginousness after oil removing of the present utility model is lower, therefore also can all feed deammoniation tower and reflux.
According to device of the present utility model, wherein, described deamination water output 10 preface successively is connected with deammoniation tower still pump 16 and deamination watercooler 17, is used to follow-up extraction process that deamination water is provided.As preferably, deamination water enters follow-up pre-extraction/extraction workshop section after deamination watercooler 17 is cooled to 35 ~ 45 ℃.
According to device of the present utility model, wherein, described ammonia lime set divides the top of oil tank 8 can be provided with lightweight oil phase delivery port 18, and the bottom can be provided with heavy oil phase delivery port 19, and described lightweight oil phase delivery port 18 all is connected with oil tank 20 with heavy oil phase delivery port 19.Lightweight oil phase in the utility model is meant the oil phase littler with respect to the density of the water in the ammonia lime set, is positioned at the water upper strata after the layering; The heavy oil phase is meant the oil phase bigger with respect to the density of water, is positioned at the lower floor of water after the layering.Like this, communicated lightweight oil phase delivery port 18 of the lightweight oil on upper strata feeds oil tanks 20, and the mink cell focus of the bottom heavy oil phase delivery port 19 that communicated feeds oil tanks.These oil can pump into light oil and go to the irrigated area to carry out processing and utilization from oil tank then, produce byproduct light oil.
According to device of the present utility model, wherein, the tube side of described one-level condensate cooler 3 can be communicated with the phenol waterpipe, is used for circulation and feeds phenol water.Because the temperature of raw material phenol water is lower, phenol water can be fed the one-level condensate cooler, with cooling depickling phenol water.
Deamination oil removal plant of the present utility model can have but be not limited to following beneficial effect:
1. this deamination oil removal plant not only can deamination, can also effectively the oil in the phenol water be removed.According to surveying and determination, when the oleaginousness in the former depickling phenol water was about 650mg/L, after this device oil removal treatment, oleaginousness can be reduced to below the 50mg/L.
2. furthermore, owing to the oleaginousness of the water that passes back into deammoniation tower is very low, can reduce or avoid the fouling or the obstruction of column plate, then also can avoid follow-up extraction process and biochemical processing process are produced detrimentally affects such as emulsification, fouling, help prolonging the overall operation cycle of equipment, improve waste water treatment efficiency, thereby also reduced processing costs.
3. in addition, but this device also by-product have ammonia and the light oil that is worth than large economy, brought extra returns to enterprise, correspondingly further reduced cost for wastewater treatment, thereby the utlity model has higher popularization and application values.
Description of drawings
Below, describe embodiment of the present utility model in conjunction with the accompanying drawings in detail, wherein:
Fig. 1 shows the process flow diagram of deamination oil removal plant of the present utility model.
Embodiment
Further specify the utility model below by specific embodiment, still, should be understood to, these embodiment are only used for the more detailed usefulness that specifically describes, and are used for limiting in any form the utility model and should not be construed as.
General description is carried out to the material and the test method that are used in the utility model test in this part.Though for realizing that employed many materials of the utility model purpose and working method are well known in the art, the utility model is still done to describe in detail as far as possible at this.It will be apparent to those skilled in the art that in context, if do not specify that the utility model material therefor and working method are well known in the art.
Below in conjunction with accompanying drawing embodiment of the present utility model is done more detailed explanation.
Fig. 1 shows the process flow diagram of deamination oil removal plant of the present utility model.This device comprises that deammoniation tower 1, the one-level condensate cooler 2, the one-level that are connected with the cat head of described deammoniation tower 1 preface successively divide flow container 3, B-grade condensation water cooler 4, secondary to divide flow container 5, three grades of condensate coolers 6 and three fraction flow containers 7, the bottom that described one-level divides flow container 3, secondary to divide flow container 5 and three fraction flow containers 7 all divides oil tank 8 to be connected with the ammonia lime set, the top of described deammoniation tower 1 is provided with depickling phenol water input 9, and the bottom is provided with deamination water output 10; The top of described three fraction flow containers is provided with ammonia delivery port 11.Those skilled in the art should know, the WCS/WCR among the figure represent respectively recirculated water (on) and recirculated water (returning).
Described deammoniation tower 1 is connected with deammoniation tower reboiler 12, is used for providing steam to carry the wet goods impurity of phenol water with gas.
Described one-level divides flow container 3 and secondary to divide flow container 5 and described ammonia lime set to divide also can be connected with ammonia lime set water cooler 13 between the oil tank 8.Like this, one-level divides liquid phase that flow container and secondary divide the flow container bottom after the cooling of ammonia lime set water cooler, can together enter the ammonia lime set with the liquid phase of the bottom of three fraction flow containers and divide oil tank.
Described ammonia lime set divides oil tank 8 to be connected with ammonia lime set pump 14, and described ammonia lime set pump 14 can be connected with gas liquor basin 15 with the top of described deammoniation tower 1 respectively.Because the aqueous phase oleaginousness after oil removing is lower, therefore also can all feed deammoniation tower and reflux, promptly described ammonia lime set pump 14 also can only be connected with the top of deammoniation tower 1.
Described deamination water output 10 preface successively is connected with deammoniation tower still pump 16 and deamination watercooler 17, is used to follow-up extraction process that deamination water is provided.
Described ammonia lime set divides the top of oil tank 8 can be provided with lightweight oil phase delivery port 18, the bottom can be provided with heavy oil phase delivery port 19, described lightweight oil phase delivery port 18 all is connected with oil tank 20 with heavy oil phase delivery port 19, can regularly collect the oil phase in the oil tank like this, with processing byproduct light oil.
The tube side of described one-level condensate cooler 3 can be communicated with the phenol waterpipe, is used for circulation and feeds phenol water, can make full use of the cold in the phenol water.
In actual use, the phenol water after depickling is handled, promptly depickling phenol water enters deammoniation tower 1 through depickling phenol water input 9 and carries out the deamination processing, and the temperature of this depickling phenol water can be preferably about 130 ℃.Described deammoniation tower can use deammoniation tower reboiler 12, adopts 1.0MPa(g), 184 ℃ steam heats.Preferably the temperature with the deammoniation tower cat head is controlled at 125 ~ 140 ℃, and tower top pressure is controlled at 0.3 ~ 0.4MPa, and tower still temperature is controlled at 150 ~ 160 ℃, and tower still pressure-controlling is at 0.35 ~ 0.45MPa.Ammonia, oil gas, water vapour and some other volatile matter are put forward by gas, form of the cat head output of thick ammonia jointly from deammoniation tower.
This thick ammonia is after 2 heat exchange of one-level condensate cooler are cooled to about 125 ~ 140 ℃, enter one-level and divide flow container 3, carry out gas-liquid separation, gas phase enters B-grade condensation water cooler 4 after the output of top, enter secondary after heat exchange is cooled to about 70 ~ 90 ℃ and divide flow container 5, after the gas-liquid separation, gas phase is from the top extraction, enter three fraction flow containers 7 after about three grades of condensate cooler 6 heat exchange to 50 ℃, after the gas-liquid separation, the ammonia of handling through three grades of condensation separation is through 11 extraction of ammonia delivery port.One-level divides liquid phase that flow container 3 and secondary divide flow container 5 bottoms after 13 coolings of ammonia lime set water cooler, can together enter the ammonia lime set with the liquid phase of the bottom of three fraction flow containers and divide oil tank 8.
Because oleaginousness is higher, the ammonia lime set is divided standing demix in the oil tank 8 in the ammonia lime set, and the lightweight oil phase is separated out on the upper strata, and bottom is separated out the heavy oil phase, is pooled in the oil tank 20 through lightweight oil phase delivery port 18 and heavy oil phase delivery port 19 respectively.The water in middle layer is after ammonia lime set pump 14 boosts, and a part can be back to deammoniation tower, and another part can loop back the gas liquor basin of gas liquor product separation.In the preferred case, because the oleaginousness of this water is very low, also can all be back to deammoniation tower.
Phenol water through deammoniation tower heat with steam gas carry etc. handle after, the deamination water of tower still is through deamination water output 10 and deammoniation tower still pump 16, be cooled to 35 ~ 45 ℃ by deamination watercooler 17 after, enter follow-up pre-extraction or extraction workshop section.
After measured, the oleaginousness of former depickling phenol water is 650mg/L, use existing installation can handle to the 200mg/L, but after device of the present utility model carried out oil removal treatment, the oleaginousness of deamination water can be reduced to below the 50mg/L.In addition, the oleaginousness that passes back into the ammonia lime set water of deammoniation tower in the existing installation is generally about 10000mg/L, can reduce to below the 1000mg/L after using this device, has all reached the ideal deoiling effect.
Although the utility model has carried out description to a certain degree, significantly, under the condition that does not break away from spirit and scope of the present utility model, can the suitable variation of each condition of carrying out.Be appreciated that the utility model is not limited to described embodiment, and belong to the scope of claim, it comprises the replacement that is equal to of described each factor.
Claims (8)
1. deamination oil removal plant, it is characterized in that, described device comprises deammoniation tower (1), the one-level condensate cooler (2) that is connected with the cat head of described deammoniation tower (1) preface successively, one-level is divided flow container (3), B-grade condensation water cooler (4), secondary divides flow container (5), three grades of condensate coolers (6) and three fraction flow containers (7), described one-level is divided flow container (3), secondary divides the bottom of flow container (5) and three fraction flow containers (7) all to divide oil tank (8) to be connected with the ammonia lime set, the top of described deammoniation tower (1) is provided with depickling phenol water input (9), and the bottom is provided with deamination water output (10); The top of described three fraction flow containers is provided with ammonia delivery port (11).
2. device according to claim 1 is characterized in that, described deammoniation tower (1) also is connected with deammoniation tower reboiler (12).
3. device according to claim 1 is characterized in that, described one-level divides flow container (3) and secondary to divide flow container (5) and described ammonia lime set to divide also to be connected with ammonia lime set water cooler (13) between the oil tank (8).
4. according to each described device in the claim 1 to 3, it is characterized in that, described ammonia lime set divides oil tank (8) to be connected with ammonia lime set pump (14), and described ammonia lime set pump (14) is connected with gas liquor basin (15) with the top of described deammoniation tower (1) respectively.
5. device according to claim 4 is characterized in that, described ammonia lime set pump (14) only is connected with the top of described deammoniation tower (1).
6. according to each described device in the claim 1 to 3, it is characterized in that described deamination water output (10) preface successively is connected with deammoniation tower still pump (16) and deamination watercooler (17), is used to follow-up extraction process that deamination water is provided.
7. according to each described device in the claim 1 to 3, it is characterized in that, described ammonia lime set divides the top of oil tank (8) to be provided with lightweight oil phase delivery port (18), the bottom is provided with heavy oil phase delivery port (19), and described lightweight oil phase delivery port (18) all is connected with oil tank (20) with heavy oil phase delivery port (19).
8. according to each described device in the claim 1 to 3, it is characterized in that the tube side of described one-level condensate cooler (3) is communicated with the phenol waterpipe, be used for circulation and feed phenol water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220727012 CN203079784U (en) | 2012-12-26 | 2012-12-26 | Deamination oil-removing device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220727012 CN203079784U (en) | 2012-12-26 | 2012-12-26 | Deamination oil-removing device |
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| Publication Number | Publication Date |
|---|---|
| CN203079784U true CN203079784U (en) | 2013-07-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220727012 Expired - Fee Related CN203079784U (en) | 2012-12-26 | 2012-12-26 | Deamination oil-removing device |
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| CN (1) | CN203079784U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106630004A (en) * | 2016-11-17 | 2017-05-10 | 内蒙古大唐国际克什克腾煤制天然气有限责任公司 | Oil removal collection device for phenol and ammonia recycling system |
| CN108854165A (en) * | 2017-12-28 | 2018-11-23 | 郑州铂来化研科技有限公司 | Oily separation method in a kind of deammoniation tower ammonia lime set |
| CN110723771A (en) * | 2019-11-07 | 2020-01-24 | 伊犁新天煤化工有限责任公司 | Novel phenol ammonia recovery device for efficiently recovering ammonia |
-
2012
- 2012-12-26 CN CN 201220727012 patent/CN203079784U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106630004A (en) * | 2016-11-17 | 2017-05-10 | 内蒙古大唐国际克什克腾煤制天然气有限责任公司 | Oil removal collection device for phenol and ammonia recycling system |
| CN108854165A (en) * | 2017-12-28 | 2018-11-23 | 郑州铂来化研科技有限公司 | Oily separation method in a kind of deammoniation tower ammonia lime set |
| CN110723771A (en) * | 2019-11-07 | 2020-01-24 | 伊犁新天煤化工有限责任公司 | Novel phenol ammonia recovery device for efficiently recovering ammonia |
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Legal Events
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130724 Termination date: 20181226 |
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| CF01 | Termination of patent right due to non-payment of annual fee |