CN107998689A - Become CO in gas acidity lime set in removing2And O2Be thermally integrated rectifying new process - Google Patents
Become CO in gas acidity lime set in removing2And O2Be thermally integrated rectifying new process Download PDFInfo
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- CN107998689A CN107998689A CN201711262168.XA CN201711262168A CN107998689A CN 107998689 A CN107998689 A CN 107998689A CN 201711262168 A CN201711262168 A CN 201711262168A CN 107998689 A CN107998689 A CN 107998689A
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- 238000000034 method Methods 0.000 title claims abstract description 43
- 235000008733 Citrus aurantifolia Nutrition 0.000 title claims abstract description 16
- 235000011941 Tilia x europaea Nutrition 0.000 title claims abstract description 16
- 239000004571 lime Substances 0.000 title claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 136
- 239000007789 gas Substances 0.000 claims abstract description 125
- 238000009833 condensation Methods 0.000 claims abstract description 36
- 230000005494 condensation Effects 0.000 claims abstract description 36
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 31
- 238000010438 heat treatment Methods 0.000 claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 27
- 238000006392 deoxygenation reaction Methods 0.000 claims abstract description 15
- 239000001257 hydrogen Substances 0.000 claims abstract description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000000446 fuel Substances 0.000 claims abstract description 13
- 238000004821 distillation Methods 0.000 claims abstract description 6
- 239000012530 fluid Substances 0.000 claims abstract description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 20
- 239000007791 liquid phase Substances 0.000 claims description 18
- 239000012071 phase Substances 0.000 claims description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 10
- 239000008213 purified water Substances 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 8
- 239000007792 gaseous phase Substances 0.000 claims description 5
- 238000001179 sorption measurement Methods 0.000 claims description 5
- 230000009466 transformation Effects 0.000 claims description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 4
- 238000000605 extraction Methods 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 239000002737 fuel gas Substances 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 238000010521 absorption reaction Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 238000004064 recycling Methods 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000005329 float glass Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0068—General arrangements, e.g. flowsheets
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0073—Degasification of liquids by a method not covered by groups B01D19/0005 - B01D19/0042
-
- 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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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention belongs to petrochemical industry device for producing hydrogen technical field, is related in a kind of removing and becomes CO in gas acidity lime set2And O2Be thermally integrated rectifying new process.Middle change airsetting liquid is removed CO by the present invention2And O2Process be changed into distillation process from steam stripping process or from flash process, and the charging of hot-fluid stock and rectifying tower reboiler are thermally integrated；The device used in technique includes middle change gas first fractional condensation tank, middle change gas second segregates tank, middle change gas the 3rd segregates tank, oxygen-eliminating device, deoxygenation water heater, demineralized-water preheater, heating agent water generator, heating agent water preheater, water recirculator, fuel air preheater, stripper, clarified water pump and stripper reboiler.The more existing common process of the present invention, CO2And O2Removing is thorough, reaches boiler feedwater standard, can directly be mixed without oxygen-eliminating device with deaerated water, reduces the load of oxygen-eliminating device；Low temperature exhaust heat recycling is abundant, saves cold and hot public work energy consumption, equipment investment and operating cost are low.
Description
Technical field
The invention belongs to petrochemical industry device for producing hydrogen field, is related in a kind of removing and becomes CO in gas acidity lime set2And O2Heat
Integrated rectifying new process.Particularly as the acid condensate liquid for being the two strands of different potential temperatures produced after middle change qi leel water, high temperature condensation
Liquid provides heat source for stripper tower bottom reboiler, then respectively enters stripper with low temperature cold lime set, by steam stripping or
CO is removed from flash distillation2And O2。
Background technology
Hydrogen is the main raw material of industry, and most important industrial gasses and special gas, is typically used as synthesis ammonia, closes
Into methanol, the raw material of synthetic hydrochloric acid, metallurgy reducing agent, hydrogen desulfurization agent etc. in petroleum refining.Hydrogen is in petrochemical industry, electronics
Industry, metallurgical industry, food processing, float glass, Minute Organic Synthesis, aerospace etc. have a wide range of applications.Work
The main method of industry hydrogen manufacturing is mostly water-gas hydrogen manufacturing or dry gas hydrogen manufacturing, and this patent becomes mainly for the medium temperature of dry gas hydrogen manufacturing device
Change workshop section.Traditional middle temperature transformation workshop section, the middle condensate liquid for becoming the generation of gas multi-stage condensing enter stripper, are stripped with water vapour de-
Except CO2And O2, subsequently enter deoxygenation groove and further remove O2, for producing steam；Ye You workshop sections do not have to steam stripping, directly according to
By the heat flash distillation removing CO of condensate liquid itself2And O2.Wherein, steam stripping is less efficient, and energy consumption is larger, and condensate liquid is certainly
Flash distillation removing CO2Effect it is not thorough enough, be easy to cause the corrosion of follow-up equipment especially deoxygenation groove, leakage accident occur.This
Outside, traditional middle temperature transformation workshop section causes larger low temperature heat waste using gas is become in water recirculator and air cooler cooling
Lose, add the energy consumption of cold public work.
The content of the invention
The present invention is directed to above-mentioned actual conditions, and it is cold that the present invention provides change gas acidity in a kind of new low energy consumption high-efficiency removing
Lime set CO2And O2Technique, by middle change airsetting liquid removing CO2And O2Process be changed into from steam stripping process or from flash process
Distillation process, and the charging of hot-fluid stock and rectifying tower reboiler are thermally integrated.Including middle change gas level-one fractional condensation tank, middle change gas two
Level fractional condensation tank, middle change gas three-level fractional condensation tank, oxygen-eliminating device, deoxygenation water heater, demineralized-water preheater, heating agent water generator, heating agent
Water preheater, water recirculator, two spare water coolers, fuel air preheater, soul water stripper, clarified water pump.Middle change
Gas enters heating agent water generator, subsequently enters middle change gas level-one fractional condensation tank.After gas-liquid separation, gas phase is heated into deaerated water
Device, enters back into middle change gas second and segregates tank.After gas-liquid separation, the liquid phase of generation segregates the liquid of tank generation with middle change gas first
Mix, enter stripper from middle part after fuel air preheater and stripper tower bottom reboiler；The gas phase of generation is passed through
Become gas the 3rd in entering after heating agent water preheater, demineralized-water preheater and water recirculator and segregate tank, gas after gas-liquid separation
Mutually enter pressure-variable adsorption part, liquid phase enters stripper from tower top.Demineralized water after preheating enters oxygen-eliminating device.After stripping
To purified water, CO2Content is down to 10ppb, O2Content reaches deoxygenation water quality standard, and therefore, purified water can be directly the same as removing after deoxygenation
Brine is mixed into follow-up steam generation facility, it is not necessary into oxygen-eliminating device, so as to reduce the energy consumption of oxygen-eliminating device.
In addition, the main function of fractional condensation tank is a point water, while make the CO dissolved in water2It is as few as possible.It is cold when high temperature segregates
Solidifying water is few, and CO at this time2Solubility in water is also small, CO in condensate liquid2Content is relatively low；When low temperature segregates, the water of condensation
Amount is more, and CO at this time2Solubility in water is also big, CO in condensate liquid2Content is higher.First tank is corresponding with last tank
Temperature be to be determined by the flow and cold public work of upstream respectively, in order to efficiently separate fractional condensation liquid and CO2, it is necessary to pass through power
The phase equilibrium relationship and CO in Hengshui2Dissolution equilibrium relation in water, determines the operation temperature and number of middle fractional condensation tank, so that
Formulation reasonably takes thermal release strategy.Specific practice is, according to middle freezing curve, the CO for becoming gas under the operating pressure2To water
The variation tendency of solubility curve, a fractional condensation tank is respectively set in the corresponding temperature of two points of inflexion on a curve.And under the operating mode, two
The corresponding temperature of bar point of inflexion on a curve approaches, therefore slave device expense and separating effect consider, and is set again between two flex points
One fractional condensation tank, three tank flows are the most reasonable altogether.
Technical scheme：
Become CO in gas acidity lime set in one kind removing2And O2Be thermally integrated rectifying new process, by middle change airsetting liquid removing CO2
And O2Process be changed into distillation process from steam stripping process or from flash process, and to the charging of hot-fluid stock and rectifying tower reboiler
It is thermally integrated；
The device used in technique includes middle change gas first and segregates tank 1, middle change gas second fractional condensation tank 2, middle the 3rd point of gas of change
Solidifying tank 3, heating agent water generator 4, deoxygenation water heater 5, heating agent water preheater 6, demineralized-water preheater 7, water recirculator 8,
Fuel air preheater 9, stripper 10, oxygen-eliminating device 11, clarified water pump 12 and stripper reboiler 13；Middle change gas feed pipe and heat
4 tube-side inlet of matchmaker's water generator is connected, and the outlet of 4 tube side of heating agent water generator segregates 1 entrance of tank with middle change gas first and is connected；Middle change
1 gaseous phase outlet of the first knockout drum of gas is connected with 5 tube-side inlet of deoxygenation water heater, liquid-phase outlet and 9 tube side of fuel air preheater
Entrance is connected；5 tube side of deoxygenation water heater is exported to be connected with the second drainer of middle change gas 2；2 gas phase of the second drainer of middle change gas goes out
Mouth is connected with 6 tube-side inlet of heating agent water preheater, and liquid-phase outlet is connected with 9 tube-side inlet of fuel air preheater；Demineralized water preheats
The outlet of 7 tube side of device is connected with 8 tube-side inlet of water recirculator, and the outlet of 8 tube side of water recirculator is segregated with middle change gas the 3rd
Tank 3 is connected；Middle change gas the 3rd segregates 3 gaseous phase outlet of tank and is connected with pressure-variable adsorption workshop section, at the top of liquid-phase outlet and stripper 10 into
Material mouth is connected；The outlet of 9 tube side of fuel air preheater is connected with 13 shell side import of stripper reboiler, 13 shell side of stripper reboiler
Outlet is connected with 10 middle part feed inlet of stripper；10 overhead extraction of stripper is connected with air, bottom of towe extraction and clarified water pump 12
Entrance is connected, and the outlet of clarified water pump 12 is connected with 11 outlet conduit of oxygen-eliminating device；7 shell-side outlet of demineralized-water preheater and oxygen-eliminating device 11
Entrance is connected, and oxygen-eliminating device 11 exports same follow-up steam generating means and is connected；
Specific embodiment is as follows：
Middle change gas becomes gas first in and segregates tank 1, the gas phase of generation is by removing after heating agent water generator 4 takes heat
After oxygen water heater 5, become the fractional condensation tank 2 of gas second in；Middle change gas first segregates tank 1 and middle change gas second segregates tank 2 and produces
Liquid phase collect after, after fuel air preheater 9 and stripper reboiler 13 take heat, enter stripper 10 from middle part；Middle change
Gas second segregates the gas phase that tank 2 produces, successively by heating agent water preheater 6, demineralized-water preheater 7 and water recirculator 8
35 DEG C are cooled to, middle change gas the 3rd is subsequently entered and segregates tank 3, gas phase is directly entered follow-up pressure-variable adsorption workshop section, and liquid phase is from top
Portion enters stripper 10；Enter oxygen-eliminating device 11 after demineralized water preheating, produce deaerated water；Purified water is produced by 10 bottom of towe of stripper,
Purified water pump 12 enters steam generation workshop section after being mixed with deaerated water；
The heating agent water generator technological parameter：Heat medium water leaving water temperature is 100 DEG C, and heat medium water additional issue amount is as freely
End, by adjusting heating agent water rate control exchanger heat load, becomes temperature degree as 155 DEG C -160 DEG C so as to control in outlet.
Middle change gas first fractional condensation 1 technological parameter of tank：Feeding temperature is 155 DEG C -160 DEG C；Operating pressure is 2.32-
2.30MPag。
Middle change gas second fractional condensation 2 technological parameter of tank：Feeding temperature is 145 DEG C -150 DEG C；Operating pressure is 2.30-
2.27MPag。
Middle change gas the 3rd fractional condensation 3 technological parameter of tank：Feeding temperature is 35 DEG C -40 DEG C；Operating pressure is 2.27-
2.25MPag。
10 technological parameter of stripper：The middle liquid phase for becoming the fractional condensation tank 3 of gas the 3rd enters from 10 tower top of stripper, middle change
Gas first segregate tank 1 and it is middle change gas second segregate 2 condensation by mixing liquid of tank after taking heat from the 2nd~3 piece of theoretical plate of stripper 10 into
Enter, operating pressure is micro-positive pressure, and 45~55 DEG C of tower top temperature, 100~110 DEG C of column bottom temperature, theoretical cam curve is 4~6 pieces；Vapour
13 load of stripper reboiler segregates tank 1 by middle change gas first and middle change gas second segregates 2 condensation by mixing liquid of tank and provides；It is net after stripping
Change water CO2Content is 10ppb, O2Content is less than 15ppb, reaches boiler feedwater standard.
The volume fraction of hydrogen is 40%~50% in the middle change gas；The volume fraction of carbon dioxide for 10%~
15%；The volume fraction of water vapour is 40%~45%；The volume fraction of methane is 2%~4%；The volume fraction of carbon monoxide
For 1%~2%；The volume fraction of residual gas is less than 1%.
Beneficial effects of the present invention：The present invention is using change gas acidity condensate liquid CO in low energy consumption high-efficiency removing2And O2New work
Skill, by middle change airsetting liquid removing CO2And O2Process be changed into distillation process from steam stripping process or from flash process, and to heat
The charging of stream stock and rectifying tower reboiler are thermally integrated.More existing common process, CO2And O2Removing is thorough, reaches boiler feedwater mark
Standard, can directly mix with deaerated water without oxygen-eliminating device, reduces the load of oxygen-eliminating device；Low temperature exhaust heat recycling is abundant, saves cold
Hot public work energy consumption.In addition, traditional handicraft is the new process by technological transformation, equipment investment and operating cost are low.
Brief description of the drawings
Fig. 1 is the process schematic representation of Zhong Bianqi workshop sections.
In figure：Become gas first in 1 and segregate tank；Become gas second in 2 and segregate tank；Become gas the 3rd in 3 and segregate tank；
4 heating agent water generators；5 deoxygenation water heaters；6 heating agent water preheaters；7 demineralized-water preheaters；
8 water recirculators；9 fuel air preheaters；10 strippers；11 oxygen-eliminating devices；12 clarified water pumps；
13 stripper reboilers.
Embodiment
Below in conjunction with the embodiment of technical solution and attached drawing, in detail the narration present invention.
Middle change gas is initially entered in heating agent water generator 4, is taken and is become gas first in entering after heat and segregate in tank 1, the gas of generation
Mutually after deoxygenation water heater 5, become the fractional condensation tank 2 of gas second in.It is pre- by fuel gas after the liquid phase that two tanks produce is collected
After hot device 9 and stripper tower bottom reboiler 13 take heat, enter stripper 10 from middle part.The middle gas second that becomes segregates the gas that tank 2 produces
Phase, is cooled to 35 DEG C by heating agent water preheater 6, demineralized-water preheater 7 and water recirculator 8, subsequently enters middle change gas
3rd fractional condensation tank 3, gas phase are directly entered follow-up pressure-variable adsorption workshop section, and liquid phase enters stripper 10 from top.Demineralized water preheats
Enter oxygen-eliminating device 11 afterwards, produce deaerated water.Purified water is produced by stripper bottom of towe, and purified water pump 12 mixes laggard with deaerated water
Enter steam generation workshop section.
Embodiment：
For certain petro-chemical corporation 25000Nm3/ h device for producing hydrogen, the middle volume fraction for becoming hydrogen in gas is 44.6%；Dioxy
The volume fraction for changing carbon is 10.9%；The volume fraction of water vapour is 40.3%；The volume fraction of methane is 2.6%；One oxidation
The volume fraction of carbon is 1.1%；The volume fraction of residual gas is 0.7%.After the present invention proposes device and method separation, only
Change CO in water2Content is 10ppb, O2Content is less than 15ppb, reaches boiler feedwater standard.
Heating agent water generator technological parameter：Heat medium water leaving water temperature is 100 DEG C, and heat medium water additional issue amount is led to as free end
Heating agent water rate control exchanger heat load is overregulated, becomes temperature degree in outlet so as to control as 156 DEG C.
Middle change gas first segregates tank technological parameter：Feeding temperature is 156 DEG C；Operating pressure is 2.30MPag.
Middle change gas second segregates tank technological parameter：Feeding temperature is 147.4 DEG C；Operating pressure is 2.28MPag.
Middle change gas the 3rd segregates tank technological parameter：Feeding temperature is 35 DEG C；Operating pressure is 2.25MPag.
Stripper technological parameter：The middle liquid phase for becoming the fractional condensation tank of gas the 3rd enters from stripper overhead, middle change gas first, second
It is 154.4 DEG C to segregate tank condensation by mixing liquid temperature degree, and temperature is 115 DEG C after taking heat, is entered from the 3rd piece of actual plate of stripper, behaviour
It is micro-positive pressure to make pressure, and 49.2 DEG C of tower top temperature, 105 DEG C of column bottom temperature, number of actual plates is 6 pieces；Tower bottom reboiler load is
423kW, segregates tank condensation by mixing liquid by middle change gas first, second and provides.Strip after-purification water CO2Content is 10ppb, O2Content
Less than 15ppb, reach boiler feedwater standard, so purified water need not enter oxygen-eliminating device, can directly be removed with what oxygen-eliminating device exported
Oxygen water mixes, and reduces the energy consumption of oxygen-eliminating device.
Become gas acidity condensate liquid CO in being removed the present invention provides a kind of low energy consumption high-efficiency2And O2New process, by middle change gas
Lime set removes CO2And O2Process be changed into distillation process by steam stripping process and from flash process, and to the charging of hot-fluid stock and
Rectifying tower reboiler is thermally integrated.More existing common process, CO2And O2Removing is thorough, reaches boiler feedwater standard, can not
Directly mixed through oxygen-eliminating device with deaerated water, reduce the load of oxygen-eliminating device；Low temperature exhaust heat recycling is abundant, saves cold and hot public work
Energy consumption.In addition, traditional handicraft is the new process by technological transformation, equipment investment and operating cost are low.
Claims (8)
1. become CO in gas acidity lime set in one kind removing2And O2Be thermally integrated rectifying new process, it is characterised in that by middle change airsetting
Liquid removes CO2And O2Process be changed into distillation process from steam stripping process or from flash process, and to the charging of hot-fluid stock and rectifying
Tower reboiler is thermally integrated；
The device used in technique includes middle change gas first and segregates tank (1), the middle change fractional condensation tank of gas second (2), middle the 3rd point of gas of change
Solidifying tank (3), heating agent water generator (4), deoxygenation water heater (5), heating agent water preheater (6), demineralized-water preheater (7), circulation
Water cooler (8), fuel air preheater (9), stripper (10), oxygen-eliminating device (11), clarified water pump (12) and stripper reboiler
(13)；It is middle change gas feed pipe be connected with heating agent water generator (4) tube-side inlet, heating agent water generator (4) tube side one outlet and
Middle change gas first segregates tank (1) entrance and is connected, another outlet of heating agent water generator (4) tube side and demineralized-water preheater (6) tube side
Entrance is connected；It is middle change the first knockout drum of gas (1) gaseous phase outlet be connected with deoxygenation water heater (5) tube-side inlet, liquid-phase outlet and
Fuel air preheater (9) tube-side inlet is connected；Deoxygenation water heater (5) tube side is exported to be connected with middle change the second drainer of gas (2)；
Middle change the second drainer of gas (2) gaseous phase outlet is connected with heating agent water preheater (6) tube-side inlet, and liquid-phase outlet is preheated with fuel gas
Device (9) tube-side inlet is connected；The outlet of demineralized-water preheater (7) tube side is connected with water recirculator (8) tube-side inlet, recirculated water
Cooler (8) tube side is exported to be connected with the middle change fractional condensation tank of gas the 3rd (3)；Middle change gas the 3rd segregates tank (3) gaseous phase outlet and transformation
Absorption workshop section is connected, and liquid-phase outlet is connected with stripper (10) its top feed mouth；Fuel air preheater (9) tube side exports and stripping
Tower reboiler (13) shell side import is connected, and stripper reboiler (13) shell-side outlet is connected with feed inlet in the middle part of stripper (10)；
Stripper (10) overhead extraction is connected with air, and bottom of towe extraction is connected with clarified water pump (12) entrance, clarified water pump (12) outlet
It is connected with oxygen-eliminating device (11) outlet conduit；Demineralized-water preheater (7) shell-side outlet is connected with oxygen-eliminating device (11) entrance, oxygen-eliminating device
(11) outlet is connected with follow-up steam generating means；
Specific embodiment is as follows：
Middle change gas becomes gas first in and segregates tank (1), the gas phase of generation is by removing after heating agent water generator (4) takes heat
After oxygen water heater (5), become the fractional condensation tank of gas second (2) in；Middle change gas first segregates tank (1) and middle change gas second segregates tank
(2) after the liquid phase produced is collected, after fuel air preheater (9) and stripper reboiler (13) take heat, vapour is entered from middle part
Stripper (10)；The middle gas second that becomes segregates the gas phase that tank (2) produces, successively by heating agent water preheater (6), demineralized-water preheater
(7) and water recirculator (8) is cooled to 35 DEG C, subsequently enters middle change gas the 3rd and segregates tank (3), gas phase is directly entered subsequently
Pressure-variable adsorption workshop section, liquid phase enters stripper (10) from top；Enter oxygen-eliminating device (11) after demineralized water preheating, produce deoxygenation
Water；Purified water is produced by stripper (10) bottom of towe, and purified water pump (12) enters steam generation workshop section after being mixed with deaerated water.
2. become CO in gas acidity lime set in a kind of removing according to claim 12And O2Be thermally integrated rectifying new process, its
It is characterized in that, described heating agent water generator (4) technological parameter：Heat medium water leaving water temperature is 100 DEG C, heat medium water additional issue amount conduct
Free end, by adjusting heating agent water rate control exchanger heat load, becomes temperature degree as 155 DEG C -160 DEG C so as to control in outlet.
3. become CO in gas acidity lime set in a kind of removing according to claim 1 or 22And O2Be thermally integrated rectifying new process,
It is characterized in that, described middle change gas first fractional condensation tank (1) technological parameter：Feeding temperature is 155 DEG C -160 DEG C；Operating pressure is
2.32-2.30MPag；
Described middle change gas second fractional condensation tank (2) technological parameter：Feeding temperature is 145 DEG C -150 DEG C；Operating pressure is 2.30-
2.27MPag；
Described middle change gas the 3rd fractional condensation tank (3) technological parameter：Feeding temperature is 35 DEG C -40 DEG C；Operating pressure is 2.27-
2.25MPag。
4. become CO in gas acidity lime set in a kind of removing according to claim 1 or 22And O2Be thermally integrated rectifying new process,
It is characterized in that, described stripper (10) technological parameter：The middle gas the 3rd that becomes segregates the liquid phase of tank (3) from stripper (10) tower top
Into middle change gas first segregates tank (1) and middle change gas second fractional condensation tank (2) condensation by mixing liquid after taking heat from stripper (10) the
2~3 pieces of theoretical plates enter, and operating pressure is micro-positive pressure, 45~55 DEG C of tower top temperature, 100~110 DEG C of column bottom temperature, theoretical tower
Plate number is 4~6 pieces；Stripper reboiler (13) load segregates tank (1) by middle change gas first and middle change gas second segregates
Tank (2) condensation by mixing liquid provides；Strip after-purification water CO2Content is 10ppb, O2Content is less than 15ppb, reaches boiler feedwater mark
It is accurate.
5. become CO in gas acidity lime set in a kind of removing according to claim 32And O2Be thermally integrated rectifying new process, its
It is characterized in that, the stripper (10) technological parameter：It is middle become gas the 3rd segregate tank (3) liquid phase from stripper (10) tower top into
Enter, middle change gas first segregates tank (1) and middle change gas second segregates tank (2) condensation by mixing liquid after taking heat from stripper (10) the 2nd
~3 pieces of theoretical plates enter, and operating pressure is micro-positive pressure, 45~55 DEG C of tower top temperature, 100~110 DEG C of column bottom temperature, theoretical tray
Number is 4~6 pieces；Stripper reboiler (13) load segregates tank (1) by middle change gas first and middle change gas second segregates tank
(2) condensation by mixing liquid provides；Strip after-purification water CO2Content is 10ppb, O2Content is less than 15ppb, reaches boiler feedwater standard.
6. become CO in gas acidity lime set in a kind of removing according to claim 1,2 or 52And O2Be thermally integrated the new work of rectifying
Skill, it is characterised in that the volume fraction of hydrogen is 40%~50% in the middle change gas；The volume fraction of carbon dioxide is
10%~15%；The volume fraction of water vapour is 40%~45%；The volume fraction of methane is 2%~4%；The body of carbon monoxide
Fraction is 1%~2%；The volume fraction of residual gas is less than 1%.
7. become CO in gas acidity lime set in a kind of removing according to claim 32And O2Be thermally integrated rectifying new process, its
It is characterized in that, the volume fraction of hydrogen is 40%~50% in the middle change gas；The volume fraction of carbon dioxide for 10%~
15%；The volume fraction of water vapour is 40%~45%；The volume fraction of methane is 2%~4%；The volume fraction of carbon monoxide
For 1%~2%；The volume fraction of residual gas is less than 1%.
8. become CO in gas acidity lime set in a kind of removing according to claim 42And O2Be thermally integrated rectifying new process, its
It is characterized in that, the volume fraction of hydrogen is 40%~50% in the middle change gas；The volume fraction of carbon dioxide for 10%~
15%；The volume fraction of water vapour is 40%~45%；The volume fraction of methane is 2%~4%；The volume fraction of carbon monoxide
For 1%~2%；The volume fraction of residual gas is less than 1%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114377438A (en) * | 2020-10-20 | 2022-04-22 | 鸿蒙科技(浙江)有限公司 | Comprehensive method for removing non-condensable gas dissolved in refrigerant |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4357882B2 (en) * | 2003-06-12 | 2009-11-04 | 正明 寺本 | Gas separation method and apparatus |
| CN102219184A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Process for preheating raw material of hydrogen production device |
| US20120279396A1 (en) * | 2011-03-15 | 2012-11-08 | Mks Instruments, Inc. | System to remove Dissolved Gases Selectively from Liquids |
| CN103508418A (en) * | 2012-06-18 | 2014-01-15 | 中国石油化工集团公司 | Start gas heating system in process of hydrogen production from water vapor and heating method |
| CN204873824U (en) * | 2015-08-21 | 2015-12-16 | 山东京博石油化工有限公司 | Device of coking dry gas hydrogen manufacturing |
-
2017
- 2017-12-04 CN CN201711262168.XA patent/CN107998689B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4357882B2 (en) * | 2003-06-12 | 2009-11-04 | 正明 寺本 | Gas separation method and apparatus |
| CN102219184A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Process for preheating raw material of hydrogen production device |
| US20120279396A1 (en) * | 2011-03-15 | 2012-11-08 | Mks Instruments, Inc. | System to remove Dissolved Gases Selectively from Liquids |
| CN103508418A (en) * | 2012-06-18 | 2014-01-15 | 中国石油化工集团公司 | Start gas heating system in process of hydrogen production from water vapor and heating method |
| CN204873824U (en) * | 2015-08-21 | 2015-12-16 | 山东京博石油化工有限公司 | Device of coking dry gas hydrogen manufacturing |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114377438A (en) * | 2020-10-20 | 2022-04-22 | 鸿蒙科技(浙江)有限公司 | Comprehensive method for removing non-condensable gas dissolved in refrigerant |
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