CN206325247U - Energy saving technique condensate liquid stripping system - Google Patents
Energy saving technique condensate liquid stripping system Download PDFInfo
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- CN206325247U CN206325247U CN201621227970.6U CN201621227970U CN206325247U CN 206325247 U CN206325247 U CN 206325247U CN 201621227970 U CN201621227970 U CN 201621227970U CN 206325247 U CN206325247 U CN 206325247U
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- process condensate
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- stripper
- pump
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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Abstract
The utility model discloses a kind of energy saving technique condensate liquid stripping system, the high-temp liquid outlet of stripper is connected by inlet channel with the liquid-inlet of hydraulic turbine unit, the liquid outlet of hydraulic turbine unit is connected by outlet conduit with the hot side import of process condensate heat exchanger, fluid level control valve is provided with inlet channel, the first valve is provided with outlet conduit, inlet channel and outlet conduit are also joined directly together by branch pipe, the second valve is provided with the branch pipe, the turbine spindle of hydraulic turbine unit is connected between the motor output shaft of the first process condensate liquid pump and pump housing axle by shaft coupling.The utility model reclaims the potential energy of stripper inner high voltage process condensate to drive process condensate pump work, the power consumption of process condensate liquid pump has been saved, so as to reach energy-saving purpose by increasing hydraulic turbine unit.
Description
Technical field
The utility model is related to a kind of energy saving technique condensate liquid stripping system, belongs to ammonia synthesis process systems technology field.
Background technology
Nitrogen fertilizer plant's ammonia synthesis process main-process stream is：Natural gas from long-distance transport pipes initially enters natural gas distribution station, day
Right gas enters the normal temperature desulphurization system of synthetic ammonia installation after gas distribution station enters row buffering and pressure regulation, then by natural gas compressing,
High temperature desulfurizing, one section of steam conversion of heat exchange type, two sections of oxygen-enriched air conversions, carbon monoxide high and low temperature conversion improves hot potash method
Decarburization, methanation deep purifying removes remaining CO and CO2, and synthesis gas compresses, ammonia synthesis under 14.0MPa, freezing separation, finally
Obtain product liquefied ammonia.
Low changing air from low changing air/desalination water- to-water heat exchanger enters low changing air separator, low changing air after heat exchange cooling
A large amount of process condensates that the inside is contained are separated inside low changing air separator, and process condensate passes through process condensate
Pump, which is forced into after 4.5-5.0MPa, enters process condensate heat exchanger, process condensate and the high-temperature liquid come out from stripper bottom
Body is exchanged heat, and fluid temperature is heated to from the top of stripper enter after 230 DEG C or so from 70 DEG C.Overheat from heating furnace
Steam (4.2MPa) is heated to after 350 DEG C to be entered from the bottom of stripper, and superheated steam is carried out in Ta Nei and process condensate
The CO2 gases contained in counter current contacting, process condensate come out after being stripped by superheated steam from stripper top.From stripping tower top
Containing mixed gas such as steam and CO2 inside the gas that portion comes out, mixed gas is finally sent to conversion procedure and steamed as technique
Vapour is used.Then process condensate temperature after stripping exports out at 250 DEG C or so from the bottom high-temp liquid of stripper
Mouthful come out, into the heat exchange of process condensate heat exchanger, process condensate after heat exchange into process condensate water cooler continue into
Row cooling, the temperature of process condensate is lowered to 50 DEG C or so and rear is finally sent to Desalting Water System by pipeline.Due to vapour
The operating pressure operating pressure of stripper is 3.5-4.2MPa, and the process condensate hydraulic coupling after stripping is very high, higher pressure
The process condensate of power, which is depressurized to after 0.3-0.4MPa, is transported to removal bitter and fishiness, and this current partial high pressure potential energy is not returned
Receive, so as to be wasted, cause a large amount of wastes of the energy.
Utility model content
In order to solve the above-mentioned technical problem, the utility model provides a kind of energy saving technique condensate liquid stripping system, rationally returns
Receive the high potential for the high-pressure process condensate liquid that stripper bottom comes out.
To achieve these goals, the technical solution of the utility model is as follows：A kind of energy saving technique condensate liquid stripping system,
Including stripper, low changing air separator, the first process condensate liquid pump, the second process condensate liquid pump, process condensate heat exchanger and
Fluid level control valve, the condensate outlet of the low changing air separator respectively with the first process condensate liquid pump and the second process condensate
The import of pump is connected, and the outlet of the first process condensate liquid pump and the second process condensate liquid pump is cold with technique by pipeline respectively
The cold side import of lime set heat exchanger is connected, and the technique on the hot side outlet of the process condensate heat exchanger and the top of stripper is cold
Lime set import is connected, and the bottom of the stripper is provided with steam inlet, and the stripper bottom is provided with high-temp liquid outlet,
It is characterized in that：The high-temp liquid outlet of the stripper is connected by inlet channel with the liquid-inlet of hydraulic turbine unit,
The liquid outlet of the hydraulic turbine unit is connected by outlet conduit with the hot side import of process condensate heat exchanger, it is described enter
It is provided with waterpipe on fluid level control valve, the outlet conduit and is provided with the first valve, the inlet channel and outlet conduit
Also it is joined directly together by branch pipe, the second valve is provided with the branch pipe, the turbine spindle of the hydraulic turbine unit passes through shaft coupling
Device is connected between the motor output shaft of the first process condensate liquid pump and pump housing axle.
Using such scheme, the high temperature high pressure liquid come out from stripper bottom first passes through hydraulic turbine unit unit phase
Even, it is driven to carry out high speed rotation when the process condensate of high pressure is by hydraulic turbine unit, process condensate is saturating by waterpower
Pressure drops to 0.3-0.4MPa after flat unit recovers energy, and the energy that hydraulic turbine unit is reclaimed with motor output shaft by being connected
Connect, driving machine pump work, by the high potential energy of recovery process condensate liquid, reach energy-saving purpose.The inlet channel
Also it is joined directly together with outlet conduit by branch pipe, the second valve is provided with the branch pipe when hydraulic turbine unit failure, it is high
Geothermal liquid can be directly entered the heat exchange of process condensate heat exchanger.
In such scheme：The cold side outlet port of the process condensate heat exchanger and the hot side import of process condensate water cooler
It is connected, process condensate by condensation brine system back off.
Beneficial effect：The utility model reclaims stripper inner high voltage process condensate by increasing hydraulic turbine unit
Potential energy drives process condensate pump work, has saved the power consumption of process condensate liquid pump, so as to reach energy-saving purpose.
Brief description of the drawings
Fig. 1 is process chart of the present utility model.
Turbine spindle that Fig. 2 is, motor output shaft, the connection diagram of pump housing axle.
Embodiment
The utility model is described in further detail with reference to the accompanying drawings and examples：
Embodiment 1, as illustrated in fig. 1 and 2：A kind of energy saving technique condensate liquid stripping system of the present utility model by stripper 1,
Low changing air separator 2, the first process condensate liquid pump 3, the second process condensate liquid pump 4, process condensate heat exchanger 5, process condensate
Liquid water cooler 6, fluid level control valve 7, the second valve 8, the first valve 9, hydraulic turbine unit 10 are constituted.
Enter from the low changing air of low changing air/desalination water- to-water heat exchanger after heat exchange cooling in low changing air separator 2, low changing air
A large amount of process condensates that face is contained are separated in the inside of low changing air separator 2.The condensate outlet of low changing air separator 2
The import with the first process condensate liquid pump 3 and the second process condensate liquid pump 4 is connected respectively, the first process condensate liquid pump 3 and second
Process condensate liquid pump 4 is in parallel, and one to open one standby.Second process condensate liquid pump 4 is stand-by pump, the first process condensate liquid pump 3 and second
The outlet of process condensate liquid pump 4 is connected by pipeline with the cold side import of process condensate heat exchanger 5 respectively, and process condensate is changed
The hot side outlet of hot device 5 is connected with the process condensate import on the top of stripper 1, and the cold side of process condensate heat exchanger 5 goes out
Mouthful it is connected with the hot side import of process condensate water cooler 6, the brine system back off of the process condensate by condensation.Stripper 1
Bottom be provided with steam inlet, the bottom of stripper 1 is provided with high-temp liquid outlet, and top sets gas vapor outlet line,
Steam after stripping removes conversion system.The liquid that the high-temp liquid outlet of stripper 1 passes through inlet channel and hydraulic turbine unit 10
Body import is connected, and the liquid outlet of hydraulic turbine unit 10 passes through the hot side import of outlet conduit and process condensate heat exchanger 5
It is connected, is provided with inlet channel on fluid level control valve 7, outlet conduit and is provided with the first valve 9, inlet channel and outlet conduit
Also it is joined directly together by branch pipe, the second valve 8 is provided with the branch pipe, the turbine spindle 10a of hydraulic turbine unit 10 passes through connection
Axle device is connected between the motor output shaft 3a of the first process condensate liquid pump 3 and pump housing axle 3b.
The utility model is not limited to above-mentioned specific embodiment, it will be appreciated that one of ordinary skill in the art is without wound
The property made work just can make many modifications and variations according to design of the present utility model.In a word, all technologies in the art
Personnel can be obtained by logical analysis, reasoning, or a limited experiment on the basis of existing technology according to design of the present utility model
The technical scheme arrived, all should be in the protection domain being defined in the patent claims.
Claims (2)
1. a kind of energy saving technique condensate liquid stripping system, including stripper (1), low changing air separator (2), the first process condensate
Pump (3), the second process condensate liquid pump (4), process condensate heat exchanger (5) and fluid level control valve (7), the low changing air separator
(2) import of the condensate outlet respectively with the first process condensate liquid pump (3) and the second process condensate liquid pump (4) is connected, described
The outlet of first process condensate liquid pump (3) and the second process condensate liquid pump (4) passes through pipeline and process condensate heat exchanger respectively
(5) cold side import is connected, and the hot side outlet and the technique on the top of stripper (1) of the process condensate heat exchanger (5) are cold
Lime set import is connected, and the bottom of the stripper (1) is provided with steam inlet, and stripper (1) bottom is provided with high-temperature liquid
Body is exported, it is characterised in that：The high-temp liquid outlet of the stripper (1) passes through inlet channel and hydraulic turbine unit (10)
Liquid-inlet is connected, and the liquid outlet of the hydraulic turbine unit (10) passes through outlet conduit and process condensate heat exchanger (5)
Hot side import be connected, be provided with the inlet channel on the fluid level control valve (7), the outlet conduit and be provided with first
Valve (9), the inlet channel and outlet conduit are also joined directly together by branch pipe, and the second valve (8) is provided with the branch pipe,
The turbine spindle of the hydraulic turbine unit (10) by shaft coupling be connected to the first process condensate liquid pump (3) motor output shaft and
Between pump housing axle.
2. energy saving technique condensate liquid stripping system according to claim 1, it is characterised in that：The process condensate heat exchanger
(5) cold side outlet port is connected with the hot side import of process condensate water cooler (6), the salt solution back off of the process condensate by condensation
System.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621227970.6U CN206325247U (en) | 2016-11-15 | 2016-11-15 | Energy saving technique condensate liquid stripping system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621227970.6U CN206325247U (en) | 2016-11-15 | 2016-11-15 | Energy saving technique condensate liquid stripping system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206325247U true CN206325247U (en) | 2017-07-14 |
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ID=59287694
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621227970.6U Active CN206325247U (en) | 2016-11-15 | 2016-11-15 | Energy saving technique condensate liquid stripping system |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854167A (en) * | 2018-09-17 | 2018-11-23 | 陕西黑猫焦化股份有限公司 | The cyclic utilization system of methane steam reforming rear condensate liquid in coke-stove gas |
| CN112097427A (en) * | 2020-10-21 | 2020-12-18 | 重庆通用工业(集团)有限责任公司 | Liquid removing system and liquid removing method of ice machine |
| CN115259259A (en) * | 2022-07-18 | 2022-11-01 | 陕西未来能源化工有限公司 | Conversion condensate treatment system and process |
| CN115585633A (en) * | 2022-11-10 | 2023-01-10 | 浙江同景冻干科技有限公司 | Freeze-drying equipment with hot water circulation recovery system |
-
2016
- 2016-11-15 CN CN201621227970.6U patent/CN206325247U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854167A (en) * | 2018-09-17 | 2018-11-23 | 陕西黑猫焦化股份有限公司 | The cyclic utilization system of methane steam reforming rear condensate liquid in coke-stove gas |
| CN108854167B (en) * | 2018-09-17 | 2023-12-05 | 陕西黑猫焦化股份有限公司 | Recycling system of condensate after methane steam conversion in coke oven gas |
| CN112097427A (en) * | 2020-10-21 | 2020-12-18 | 重庆通用工业(集团)有限责任公司 | Liquid removing system and liquid removing method of ice machine |
| CN112097427B (en) * | 2020-10-21 | 2024-03-08 | 重庆通用工业(集团)有限责任公司 | Liquid removing system and liquid removing method of ice machine |
| CN115259259A (en) * | 2022-07-18 | 2022-11-01 | 陕西未来能源化工有限公司 | Conversion condensate treatment system and process |
| CN115585633A (en) * | 2022-11-10 | 2023-01-10 | 浙江同景冻干科技有限公司 | Freeze-drying equipment with hot water circulation recovery system |
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