CN203295307U - High-temperature condensed water treatment device of petroleum refining industry - Google Patents
High-temperature condensed water treatment device of petroleum refining industry Download PDFInfo
- Publication number
- CN203295307U CN203295307U CN2012205867635U CN201220586763U CN203295307U CN 203295307 U CN203295307 U CN 203295307U CN 2012205867635 U CN2012205867635 U CN 2012205867635U CN 201220586763 U CN201220586763 U CN 201220586763U CN 203295307 U CN203295307 U CN 203295307U
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- Prior art keywords
- condensed water
- interchanger
- water
- stage heat
- stage
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 124
- 238000005504 petroleum refining Methods 0.000 title abstract 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 8
- 239000001301 oxygen Substances 0.000 claims abstract description 8
- 239000003921 oil Substances 0.000 claims description 38
- 238000007670 refining Methods 0.000 claims description 10
- 238000005276 aerator Methods 0.000 claims description 8
- 239000011347 resin Substances 0.000 claims description 4
- 229920005989 resin Polymers 0.000 claims description 4
- 238000004945 emulsification Methods 0.000 claims description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052742 iron Inorganic materials 0.000 abstract description 3
- 150000001875 compounds Chemical class 0.000 abstract 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 230000003020 moisturizing effect Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000006392 deoxygenation reaction Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000002242 deionisation method Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229910001447 ferric ion Inorganic materials 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910001410 inorganic ion Inorganic materials 0.000 description 1
- 239000010954 inorganic particle Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- -1 iron ion Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229960001866 silicon dioxide Drugs 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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Abstract
The utility model discloses a high-temperature condensed water treatment device of petroleum refining industry. The high-temperature condensed water treatment device comprises five parts which are respectively a three-stage heat exchange device, a high-efficiency filter device, a high-efficiency oil removing device, a compound iron removing device and an oxygen removing device, wherein the three-stage heat exchange device comprises three groups of first-stage heat exchangers, second-stage heat exchangers and third-stage heat exchangers and the three groups of first-stage heat exchangers, second-stage heat exchangers and third-stage heat exchangers, are used for respectively receiving the high-temperature condensed water; cold water input of the first-stage heat exchangers is communicated with condensed water output of the second-stage heat exchangers; the cold water input of the second-stage heat exchangers is communicated with the condensed water output of the third-stage heat exchanger heat exchange device; the cold water output of the first-stage heat exchangers is communicated with the oxygen removing device; hot water output of the third-stage heat exchangers sequentially enters the high-efficiency filter device, the high-efficiency oil removing device and the compound iron removing device.
Description
Technical field
The utility model is about a kind of condensed water in high temperature treatment unit of oil refining industry.
Background technology
The condensed water in high temperature of oil refining industry is the steam condenses that produces on oil refining technique, the processing mode of the present refinery of this steam condenses is generally by recycling after water cooling tower, the condensed water that reclaims can be got back to the moisturizing of Low Temperature Thermal device in the winter time, can be back to use circulating water system in summer,, there is the problem of " high-quality low use " in moisturizing as recirculated water., due to the shortage of fund and technique means, still have the part refinery that condensed water is carried out in line in addition, seriously cause the waste of water resources and thermal source.
Summary of the invention
The purpose of this utility model is to provide a kind of condensed water in high temperature treatment unit of oil refining industry, utilizes this device that condensed water is recycled, and the recovery that effectively improves condensed water in high temperature is personal, has improved the service efficiency of heat energy.
the condensed water in high temperature treatment unit of the oil refining industry in the utility model includes five parts, be respectively: three grades of heat-exchanger rigs, effective filter, efficient oil removing apparatus, deferrization device and de-aerator plant, described three grades of heat-exchanger rigs include three groups and receive respectively condensed water in high temperature first step interchanger, second stage interchanger and third stage interchanger, the cold water input of first step interchanger is communicated with the condensed water output of second stage interchanger, the cold water input of second stage interchanger is communicated with the condensed water output of third stage interchanger heat-exchanger rig, the cold water output of described first step interchanger is communicated with described de-aerator plant, the hot water output of described third stage interchanger enters effective filter successively, efficient oil removing apparatus, the deferrization device.
Be provided with the condensed water surge tank between the hot water output of described effective filter and described third stage heat-exchanger rig.
Fill oil removing in described efficient oil removing apparatus resin dedicated, will, by automatically separating after the oils emulsification droplet coarse in the condensed water of high efficiency filter output, be gathered in the top of efficient oil removing apparatus.
Described de-aerator plant includes deoxygenator, and described deoxygenator is selected rotary film scavenge oxygen equipment.
Description of drawings
Fig. 1 is the schematic flow sheet of condensed water in high temperature treatment unit in the utility model.
Fig. 2 is the structural representation of condensed water in high temperature treatment unit in the utility model.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the utility model is elaborated.
Condensed water in high temperature treatment unit in the utility model includes five parts, is respectively: three grades of heat-exchanger rigs, effective filter 6, efficient oil removing apparatus 7, deferrization device 8 and de-aerator plants 12.Wherein:
Three grades of heat-exchanger rigs include first step interchanger 1, second stage interchanger 2 and third stage interchanger 3.From the vapor condenses water temp of refinery output up to 147.8 ℃, at first the condensed water that is flash tank V2/V3 output enters in the interior delivery pipeline of first step interchanger 1, simultaneously cold water is inputted in first step interchanger 1, made hot water and cold water in the delivery pipeline carry out heat exchange.Make the temperature of cold water be heated to 84.5 ℃ of left and right, the hot water temperature in the delivery pipeline is down to 88 ℃ of left and right.
From the temperature of the delivery pipeline of first step interchanger 1 output in the condensed water of 88 ℃ of left and right and the delivery pipeline that enters after the condensed water of flash tank V1 output temperature up to 104.6 ℃ mixed by line mixer in second stage interchanger 2, cold water is inputted in second stage interchanger 2 simultaneously, make cool water heating to the 71.6 ℃ left and right of input, the hot water temperature in the delivery pipeline is down to 70 ℃ of left and right.The temperature of second stage interchanger 2 outputs is the cold water that the cold water of 71.6 ℃ of left and right is used for input first step interchanger 1.
Enter the delivery pipeline of third stage interchanger from the condensed water of temperature 70 ℃ of left and right of second stage interchanger 2 delivery pipeline outputs 67.3 ℃ of left and right with temperature temperature after the large aromatics process of 65 ℃ of left and right mixes by line mixer with steam condenses, the third stage of cold water input simultaneously interchanger 3 also is heated to 62.7 ℃ of left and right, enters condensed water surge tank 4 after the hot water temperature in the delivery pipeline is down to 60 ℃ of left and right again.The cold water of the temperature of third stage interchanger 3 outputs 62.7 ℃ of left and right is used for the cold water of input second stage interchanger 2.The cold water of input third stage interchanger 3 is the condensed water after follow up device is processed of third stage interchanger 3 delivery pipeline outputs.
The condensed water that enters in condensed water surge tank 4 enters effective filter 6 after condensed water buffering pump 5 boosts, remove particle diameter ferriferous oxide and other mechanical impurity greater than 5um, for the subsequent disposal unit provides qualified condensed water.In the utility model, the condensed water in high temperature treatment unit is provided with 3 (concrete quantity can arrange according to demand) high efficiency filters 6, every in-built 4 high-throughput secondary filter cores.At the forward and backward tensimeter that is provided with of high efficiency filter 6, in order to observe the operation conditions of high efficiency filter 6, pressure reduction and pressure change by before and after analyzing, judge whether more renew cartridge.The end cover structure of high efficiency filter adopts and opens soon the formula design, makes the work of renew cartridge more more convenient, and this is easily to realize to one skilled in the art, therefore no longer explanation explanation.
Directly enter efficient oil removing apparatus 7 from the water of high efficiency filter 6 outputs; fill oil removing in efficient oil removing apparatus 7 resin dedicated; to, by automatically separating after the oils emulsification droplet coarse in the condensed water of high efficiency filter 6 outputs, be gathered in the top of efficient oil removing apparatus 7.According to program setting, regularly automatically open the oil drain solenoid valve on efficient oil removing apparatus 7, isolated oil is expelled to waste oil pool.
The utility model can arrange 7,6 operations simultaneously of 6 efficient oil removing apparatus, the separation that effectively improves profit.Each efficient oil removing apparatus is provided with into water valve, outlet valve, goes out the valves such as water discharging valve, vent valve, manual draining valve.Be provided with in addition and rinse into water valve, flushing bleed valve, can rinse device where necessary.Efficient oil removing apparatus 7 is equipped with the instrument of controlling and observing for operation, as pressure transmitter, thermometer etc. and signal is sent into the DCS system.
Enter deferrization device 8 from efficient oil removing apparatus 7 output condensed water, iron ion, silicon and other micro ion in removal water are by the ion exchange resin adsorbing and removing.Deferrization device in the utility model is provided with 4,3 and uses simultaneously, and 1 standby.After wherein a cover deferrization device cycle of operation end was lost efficacy, stand-by plant will put into operation automatically according to the setting of program, and disabling device will automatically rinse and regenerate, and recover to enter stand-by state after deironing, desalination ability.
Qualified water after deironing enters third stage interchanger 3 after intermediate water tank 10 and middle water pump 11, as the cold water of exchange, deferrization device 8 output water are after the on-line detector table analysis, and underproof water is back to condensed water buffering water pot 4 and again processes.
de-aerator plant includes deoxygenator 12, be used for receiving the cold water (call clean water) of the temperature of first step interchanger output 84.5 ℃ of left and right, adopt high pressure heating power deoxyprocess, condensed water after processing with 1.0MPa steam is heated to the temperature of saturation corresponding with the deoxygenator internal pressure, according to henry's law and Dalton's law, utilize dissolving the relying on property of gas in water, the non-cold wet bodies such as the oxygen and carbon dioxide that is dissolved in the water are separated out in water, enter atmosphere by the top vapor pipe, make the oxygen level in water reach specified standards, qualified deaerated water is stored in the needs of preparing at any time oiler feed in the water tank of deoxygenator bottom.Clean water enters deoxygenator, and steam enters deoxygenator by a cover by the pressure controlled variable valve group of deoxygenator, with the clean moisture film that descends, fully contacts, and realizes thermal de-aeration.Deaeration plant is selected rotary film scavenge oxygen equipment.Be comprised of membrane deaerator, deaerator storage tank and annex,, by water (flow) direction, from top to bottom be divided into exhaust section, skinning device group, space section, shutter grate layer, packing layer, vapour distributor and deoxygenation water tank form.
Deaerated water in the deoxygenation water tank is supplied with power plant through the deaerated water pump delivery and is used as boiler feedwater.
Because high-duty boiler supply water quality requirement pH value is 9.0 ~ 9.6, so the condensed water after processing must be regulated the pH value when being delivered to boiler feed, the utility model is provided with 1 cover Automatic Ammonia adding device 14, the volume pump of ammonifying device, by Frequency Converter Control, can be regulated ammonia residual automatically according to the pH value of condensed water in water supply line.Establish wash water valve in ammonia solution case bottom, Y-filter is established in outlet.
In sum, the particle diameter that utilizes condensed water device in the utility model to remove to exist in the condensed water is greater than 5um inorganic particle material, oil, ferric ion, silicon-dioxide (SiO
2), inorganic ion and dissolved oxygen, make water outlet can reach medium pressure boiler moisturizing water quality requirement, saved Boiler water Feeding System system (de-mineralized water treatment system).Make the heat utilization rate of condensed water in high temperature reach 90%,, because the resin in oil-removing iron-removing apparatus requires medium temperature less than 80 ℃,, so adopt three grades of heat-exchanger rigs, make the condensed water two-direction heat-exchanging.Qualified condensed water in high temperature enters heat-exchanger rig, temperature is reduced to 60 ℃ after heat exchange, de-mineralized water after cooling enters the condensate fine treating part, the low temperature de-mineralized waters that 57 ℃ of condensed water after the oil removing deionization are mixed trace make temperature be reduced to cold side that 55 ℃ of laggard entering plates change the condensed water in high temperature of hot side to be carried out heat exchange, reclaim the heat of condensed water in high temperature.
Claims (4)
1. the condensed water in high temperature treatment unit of an oil refining industry includes five parts, be respectively: three grades of heat-exchanger rigs, effective filter, efficient oil removing apparatus, deferrization device and de-aerator plant, it is characterized in that, described three grades of heat-exchanger rigs include three groups and receive respectively condensed water in high temperature first step interchanger, second stage interchanger and third stage interchanger, the cold water input of first step interchanger is communicated with the condensed water output of second stage interchanger, the cold water input of second stage interchanger is communicated with the condensed water output of third stage interchanger heat-exchanger rig, the cold water output of described first step interchanger is communicated with described de-aerator plant, the hot water output of described third stage interchanger enters effective filter successively, efficient oil removing apparatus, the deferrization device.
2. the condensed water in high temperature treatment unit of oil refining industry according to claim 1, is characterized in that, is provided with the condensed water surge tank between the hot water output of described effective filter and described third stage heat-exchanger rig.
3. the condensed water in high temperature treatment unit of oil refining industry according to claim 1; it is characterized in that; fill oil removing in described efficient oil removing apparatus resin dedicated; to, by automatically separating after the oils emulsification droplet coarse in the condensed water of high efficiency filter output, be gathered in the top of efficient oil removing apparatus.
4. the condensed water in high temperature treatment unit of oil refining industry according to claim 1, is characterized in that, described de-aerator plant includes deoxygenator, and described deoxygenator is selected rotary film scavenge oxygen equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205867635U CN203295307U (en) | 2012-11-08 | 2012-11-08 | High-temperature condensed water treatment device of petroleum refining industry |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205867635U CN203295307U (en) | 2012-11-08 | 2012-11-08 | High-temperature condensed water treatment device of petroleum refining industry |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203295307U true CN203295307U (en) | 2013-11-20 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2012205867635U Expired - Lifetime CN203295307U (en) | 2012-11-08 | 2012-11-08 | High-temperature condensed water treatment device of petroleum refining industry |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104671495A (en) * | 2013-12-02 | 2015-06-03 | 逸盛大化石化有限公司 | Water recycling system in PTA (pure terephthalic acid) production process |
| CN105972580A (en) * | 2016-06-22 | 2016-09-28 | 天津安联天源节能科技有限公司 | Recycling device capable of detecting steam condensate water quality |
| CN108609777A (en) * | 2018-06-28 | 2018-10-02 | 中电环保股份有限公司 | A kind of the petrochemical industry lime set processing system and processing method of high temperature oil removing |
| CN116040716A (en) * | 2022-09-28 | 2023-05-02 | 江苏华晖环保科技有限公司 | New energy evaporation condensate treatment process |
-
2012
- 2012-11-08 CN CN2012205867635U patent/CN203295307U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104671495A (en) * | 2013-12-02 | 2015-06-03 | 逸盛大化石化有限公司 | Water recycling system in PTA (pure terephthalic acid) production process |
| CN104671495B (en) * | 2013-12-02 | 2016-06-08 | 逸盛大化石化有限公司 | Water circulation utilization system in PTA production process |
| CN105972580A (en) * | 2016-06-22 | 2016-09-28 | 天津安联天源节能科技有限公司 | Recycling device capable of detecting steam condensate water quality |
| CN108609777A (en) * | 2018-06-28 | 2018-10-02 | 中电环保股份有限公司 | A kind of the petrochemical industry lime set processing system and processing method of high temperature oil removing |
| CN116040716A (en) * | 2022-09-28 | 2023-05-02 | 江苏华晖环保科技有限公司 | New energy evaporation condensate treatment process |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20131120 |
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| CX01 | Expiry of patent term |