CN102718184A - System and method for recycling waste glycerol to produce hydrogen by using heating furnace flue gas - Google Patents
System and method for recycling waste glycerol to produce hydrogen by using heating furnace flue gas Download PDFInfo
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- CN102718184A CN102718184A CN2011100778141A CN201110077814A CN102718184A CN 102718184 A CN102718184 A CN 102718184A CN 2011100778141 A CN2011100778141 A CN 2011100778141A CN 201110077814 A CN201110077814 A CN 201110077814A CN 102718184 A CN102718184 A CN 102718184A
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- Prior art keywords
- flue
- sorbent material
- glycerine
- hydrogen
- preheater
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- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 title claims abstract description 174
- 239000001257 hydrogen Substances 0.000 title claims abstract description 57
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 56
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 46
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 20
- 239000003546 flue gas Substances 0.000 title claims abstract description 20
- 238000010438 heat treatment Methods 0.000 title claims abstract description 15
- 238000000034 method Methods 0.000 title claims description 35
- 238000004064 recycling Methods 0.000 title abstract description 5
- 239000002699 waste material Substances 0.000 title abstract description 4
- 239000007789 gas Substances 0.000 claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 claims abstract description 14
- 238000011084 recovery Methods 0.000 claims abstract description 13
- 239000007864 aqueous solution Substances 0.000 claims abstract description 11
- 235000011187 glycerol Nutrition 0.000 claims description 81
- 239000002594 sorbent Substances 0.000 claims description 40
- 239000000243 solution Substances 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 230000008569 process Effects 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 19
- 238000005098 hot rolling Methods 0.000 claims description 9
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 229910003023 Mg-Al Inorganic materials 0.000 claims description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 2
- 239000002250 absorbent Substances 0.000 claims description 2
- 230000002745 absorbent Effects 0.000 claims description 2
- 230000004913 activation Effects 0.000 claims description 2
- GDVKFRBCXAPAQJ-UHFFFAOYSA-A dialuminum;hexamagnesium;carbonate;hexadecahydroxide Chemical compound [OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Al+3].[Al+3].[O-]C([O-])=O GDVKFRBCXAPAQJ-UHFFFAOYSA-A 0.000 claims description 2
- 239000010881 fly ash Substances 0.000 claims description 2
- 239000008246 gaseous mixture Substances 0.000 claims description 2
- 229960001545 hydrotalcite Drugs 0.000 claims description 2
- 229910001701 hydrotalcite Inorganic materials 0.000 claims description 2
- 239000012535 impurity Substances 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 229910052700 potassium Inorganic materials 0.000 claims description 2
- 239000011591 potassium Substances 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 claims 1
- 239000002918 waste heat Substances 0.000 abstract description 7
- -1 hydrogen Chemical class 0.000 abstract description 2
- 239000003463 adsorbent Substances 0.000 abstract 3
- 239000000779 smoke Substances 0.000 description 10
- 150000002431 hydrogen Chemical class 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 230000008859 change Effects 0.000 description 6
- 238000005868 electrolysis reaction Methods 0.000 description 5
- 239000003517 fume Substances 0.000 description 5
- 239000000428 dust Substances 0.000 description 3
- 238000005461 lubrication Methods 0.000 description 3
- 239000012451 post-reaction mixture Substances 0.000 description 3
- AMQJEAYHLZJPGS-UHFFFAOYSA-N N-Pentanol Chemical compound CCCCCO AMQJEAYHLZJPGS-UHFFFAOYSA-N 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 230000008901 benefit Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- 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
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a system and a method for producing hydrogen by recovering waste glycerol by using flue gas of a heating furnace, which are characterized in that a waste heat recovery system is arranged at an inlet of a horizontal flue of a conventional hot-rolled plate blank heating furnace, the system comprises a glycerol aqueous solution preheater, an emitter, a reactor and a solid-gas separator, wherein the glycerol aqueous solution preheater and a CO aqueous solution are used for recycling hydrogen2The adsorbent preheater is arranged above the flue inlet of the heating furnace in parallel, the adsorbent preheater and the adsorbent preheater are respectively connected with the emitter arranged at the bottom of the flue inlet (in the flue) through the connecting pipeline, and the reactor, the solid-gas separator and the emitter are arranged in the flue.
Description
Technical field
The present invention relates to the recycling of the useless glycerine of machinery lubrication system, relates in particular to the system and the recovery method that utilize the useless glycerine of conventional hot rolling slab process furnace horizontal flue ingress flue gas waste heat recovery to produce clear energy sources hydrogen.
Background technology
In various commercial runs, be used for the lubricated glycerine of various mechanical systems and often can not be dissipated fully by system, there is surplus, these superfluous useless glycerine directly are discharged in the environment, have both wasted resource, again contaminate environment.
In all kinds of waste resource reutilization technologies; The recovery of the useless glycerine of solid does not receive enough attention of researchist, for more existing recovery technologies, owing to consider the direct utilization of useless glycerine isolatedly; Expense is bigger; Operability is not strong, as: a kind of method that from the waste water appearance liquid that contains very small amount of glycerine, reclaims glycerine (sees that domestic patent " reclaims glycerine ", the patent No.: CN85109000) from brine waste; This method is passed through when reclaiming glycerine: evaporate, contact with amylalcohol, separate salt, the flash distillation of separating out and remove amylalcohol, five links of rectification under vacuum; Flow process is comparatively complicated, and cost of investment is high, is not suitable for not consuming in the greasing recovery of clean useless glycerine.
Conventional hot rolling slab process furnace flue entrance place flue-gas temperature is between 800 ℃～950 ℃; Way of recycling for this type fume afterheat is normally put one to two group of air heat exchanger at horizontal flue, behind air heat exchanger, adds one group of gas change heater (process furnace that has does not have gas change heater) again coal gas is carried out preheating.In actual use, because funnel temperature is too high, sky, gas change heater in the horizontal flue are easy to burn out, and the life-span of interchanger is generally about 2 years under this condition.Be head it off, way commonly used is to add a typhoon machine to purge in the horizontal flue ingress, reduces inlet flue gas temperature, and heat exchanger entrance place flue-gas temperature is reduced between 600 ℃～700 ℃, and this method can guarantee that the life-span of interchanger maintained about 5 years.But shortcoming is the energy level that has reduced fume afterheat, has increased the electric consumption of blower fan.Therefore be necessary that development new technologies reclaim this partial fume waste heat.
In the new preparation technology of existing all kinds of hydrogen; Two main schools are arranged from the angle of energy expenditure: the one, consumed power; Commonly use the hydrogen production process of brine electrolysis; (patent No.: CN200820218961.X), this patent provides a kind of water electrolysis hydrogen production device like patent " water electrolysis hydrogen production device ".This device can reclaim producing the electric weight that hydrogen consumes, and makes the electrolyzer required voltage that produces electrolysis again with the electric weight that reclaims, and so repeatedly, can reduce the spent electric energy of electrolysis greatly.But the essence of its consumed power does not change.Two, consume heat energy, (patent No.: CN200810302074.5), it is 500 ℃～660 ℃ that this patent provides the hydrogen production process temperature of reaction, keeps a large amount of thermal source of this reaction needed dissipation like patent " a kind of method of utilizing the hydrogen manufacturing of catalyzer cracking regenerated flue gas ".These two types of hydrogen producing technologies all are in a large amount of a kind of energy that dissipate, to obtain the another kind of energy.Whole process has comprised the reduction of energy level and then has raise two processes.Therefore, should not in isolated system, prepare hydrogen, can the reactive system of hydrogen manufacturing be positioned in the aforesaid flue system, the reactor drum that is about to glycerine hydrogen manufacturing is as waste-heat recovery device.
Summary of the invention
The present invention discloses a kind of system and recovery method that utilizes flue gas of heating furnace to reclaim useless glycerine hydrogen manufacturing; The rerum natura of utilizing glycerine to have infinitely to dissolve each other with water and the aqueous solution of glycerine can be used as the preparation raw material two big characteristics of clear energy sources hydrogen; Reclaim with useless glycerine lubricated, be mixed with aqueous glycerin solution, and utilize conventional hot rolling slab process furnace horizontal flue ingress fume afterheat resource that the discarded glycerine of machinery lubrication system after reclaiming is carried out advanced treatment and produce clear energy sources hydrogen; Avoid directly recycling the required loaded down with trivial details technology of glycerine; Through the fume afterheat effect, convert it into clear energy sources hydrogen, thereby realize the comprehensive utilization of useless glycerine.
Characteristics of the present invention are that residual neat recovering system is installed in conventional hot rolling slab process furnace horizontal flue ingress, and this position flue-gas temperature scope is 800 ℃～950 ℃, and this system comprises aqueous glycerin solution preheater, CO
2Sorbent material preheater, projector, reactor drum and solid-5 chief components such as gas separating device are installed CO above the projector of the flue outside
2Sorbent material adding set and CO
2The sorbent material preheating unit.
Process step of the present invention is following: at first solid-state discarded glycerine is collected; And utilize glycerine can carry out the dissolved characteristics with any ratio with water; With the useless glycerine of collecting be mixed with glycerine and hydromassage you than the aqueous solution that is 1: 4～7; And this solution is heated to 65 ℃～75 ℃, filter then and remove impurity and obtain pure aqueous glycerin solution; It is 1: 8.9～9.3 aqueous solution that this aqueous glycerin solution is added the mol ratio that is mixed with glycerine and water behind the water, and pump carries out preheating to the glycerine preheating unit that places flue, simultaneously with CO
2Sorbent material imports to the preheater that places flue and carries out preheating from its adding set, both preheating temperature scopes are 510 ℃～530 ℃, CO
2Sorbent material is that particle diameter is the potassium activation Mg-Al based hydrotalcite of 38～180 μ m; With aqueous glycerin solution after the preheating and CO
2Sorbent material imports in the projector, in projector, mixes, and feeds then in the reactor drum, and following reaction takes place in reactor drum:
C
3H
8O
3+3H
2O＝3CO
2+7H
2，ΔH
298＝128kJ/mol，
Temperature of reaction is 527 ℃～577 ℃, the CO in the resultant of reaction
2With CO
2Sorbent reactions, the catalyzer that reaction is adopted is a nickel, catalyzer is reusable through regeneration, catalyst activity area＞70.00m2/g, the active time is 6～7 hours; The pressure condition of reaction is 1 normal atmosphere, and the flow velocity of aqueous glycerin solution is 0.4～0.7m/s, and the mass ratio of aqueous glycerin solution and sorbent material is 1: 3.1～3.3.Reactor drum is two groups, one group of more another group work during catalyst changeout.Thereafter, resultant of reaction and CO
2In solid-gas separating device, rely on sorbent material absorbent particles and gaseous mixture proportion different characteristic realize that solid, gas separates, and separate back gaseous product (for hydrogen and water vapor) and obtain clear energy sources hydrogen after the water treatment and be stored in the hydrogen cylinder through removing.CO
2Sorbent material is collected in the sorbent material scoop after going out fly-ash separator, and sorbent material can be recycled through regeneration.
The present invention is through the comprehensive utilization to useless glycerine of solid and conventional bar plate heating stove horizontal flue ingress waste heat; Useless glycerine that machinery lubrication system do not dissipate directly discharging and the environmental pollution and the wasting of resources that cause have been avoided; Realized conventional bar plate heating stove horizontal flue ingress flue gas waste heat recovery simultaneously; And this part energy is converted into the high level hydrogen energy source by the waste heat form of low-lying level, have good economic worth and social benefit.
Description of drawings
Accompanying drawing reclaims useless glycerine hydrogen generating system synoptic diagram for the present invention utilizes flue gas of heating furnace.
Among the figure: 1 solid-state useless glycerine, 2 is that the clean aqueous glycerin solution, 3 of question response is that glycerine preheater, 4 is CO
2Sorbent material adding set, 5 is CO
2Sorbent material preheating unit, 6 projectors, 7 are that reactor drum, 8 is that solid-gas separating device, 9 is that hydrogen cylinder, 10 is CO
2Sorbent material collection device, 11 is process furnace horizontal flue inlet.
Embodiment
Below in conjunction with accompanying drawing embodiments of the invention are described in detail.
The present invention installs residual neat recovering system at conventional hot rolling slab process furnace horizontal flue 11 places that enter the mouth, and this system mainly comprises aqueous glycerin solution preheater 3, CO
2Sorbent material preheater 5, projector 6, reactor drum 7 and solid-gas separating device 8 are with aqueous glycerin solution preheater and CO
2The parallel process furnace flue entrance top that is installed on of sorbent material preheater; The two is all placed perpendicular to horizontal direction; And link to each other with the projector that places the flue entrance bottom through connecting tube respectively; The same with the projector flue that all places with solid-gas separating device of reactor drum is inner, and links to each other successively through connecting tube, and the modes of emplacement of the two all guarantees also that perpendicular to horizontal direction solid-gas separates.
For providing system response required CO continuously
2Sorbent material is installed CO above the projector of the flue outside
2Sorbent material adding set 4 and CO
2Sorbent material preheating unit 5.
Instance 1: fetch the useless glycerine of 100kg of receipts, its mass concentration is 92%, and then its amount that contains pure glycerin is 1000mol, in this glycerine, adds 7000mol (126kg) water, filters the aqueous glycerin solution that obtains having certain purity through leaving standstill.This aqueous solution is heated to 75 ℃, and filters and obtain purified aqueous glycerin solution.The loss of water is 100mol in the said process.
As shown in the figure; Residual neat recovering system provided by the invention is installed on conventional hot rolling slab process furnace horizontal flue 11 places that enter the mouth; This class A furnace A chimney bottom draft is-400～-300Pa between, single group resistance empty, gas change heater is usually less than 100Pa, after the horizontal flue inlet is put into the hydrogen production reaction system; Because its inside needs heating fluent meterial (aqueous glycerin solution); Its volume must than empty, gas change heater is little a lot of to the resistance of flue gas, so three's resistance can not surpass the required draft of smoke evacuation with value, promptly adding hydrogen generating system does not influence the process furnace smoke evacuation.Flue-gas temperature is 950 ℃, and temperature of reaction is 577 ℃, and the flow velocity of aqueous glycerin solution is 0.7m/s, and the amount that adds entry in the aqueous glycerin solution is that its molar concentration rate is 1: 9.3 after 2400 moles.Aqueous glycerin solution and CO
2The sorbent material preheating temperature is 530 ℃, feeds in the reactor drum through projector then and reacts, and post reaction mixture realizes hydrogen, vaporous water and CO in tornado dust collector
2Sorbent material separates.Behind hydrogen and the vaporous water smoke outlet flue, owing to receive the influence of temperature drop, water is realized separating with hydrogen, and hydrogen is collected in the hydrogen cylinder, and the amount of hydrogen is 7000 moles.CO
2Collect in the scoop behind the sorbent material smoke outlet flue, recycle after the regeneration.
Fetch the useless glycerine of the 115kg of receipts, its mass concentration is 80%, and then its amount that contains pure glycerin is 1000mol, in this glycerine, adds 7000mol (126kg) water, filters the aqueous glycerin solution that obtains having certain purity through leaving standstill.This aqueous solution is heated to 70 ℃, and filters and obtain purified aqueous glycerin solution.The loss of water is 100mol in the said process.
By the present technique scheme residual neat recovering system is installed on conventional hot rolling slab process furnace horizontal flue ingress; Of instance 1; This place does not influence the process furnace smoke evacuation after adding device for producing hydrogen; Preheating temperature is 520 ℃, feeds in the reactor drum through projector then and reacts, and post reaction mixture realizes hydrogen, vaporous water and CO in tornado dust collector
2Sorbent material separates.Behind hydrogen and the vaporous water smoke outlet flue, owing to receive the influence of temperature drop, water is realized separating with hydrogen, and hydrogen is collected in the hydrogen cylinder, and the amount of hydrogen is 7000 moles.CO
2Collect in the scoop behind the sorbent material smoke outlet flue, recycle after the regeneration.
Fetch the useless glycerine of 126kg of receipts, its mass concentration is 73%, and then its amount that contains pure glycerin is 1000mol, in this glycerine, adds 7000mol (126kg) water, filters the aqueous glycerin solution that obtains having certain purity through leaving standstill.This aqueous solution is heated to 65 ℃, and filters and obtain purified aqueous glycerin solution.The loss of water is 100mol in the said process.
Residual neat recovering system provided by the invention is installed on conventional hot rolling slab process furnace horizontal flue ingress; Of instance 1; This place does not influence the process furnace smoke evacuation after adding device for producing hydrogen, and flue-gas temperature is 800 ℃, and temperature of reaction is 527 ℃; The flow velocity of aqueous glycerin solution is 0.4m/s, and the amount that adds entry in the aqueous glycerin solution is that its volumetric molar concentration is 1: 8.9 after 2000 moles.Aqueous glycerin solution and CO
2The sorbent material preheating temperature is 510 ℃, feeds in the reactor drum through projector then and reacts, and post reaction mixture realizes hydrogen, vaporous water and CO in tornado dust collector
2Sorbent material separates.Behind hydrogen and the vaporous water smoke outlet flue, owing to receive the influence of temperature drop, water is realized separating with hydrogen, and hydrogen is collected in the hydrogen cylinder, and the amount of hydrogen is 7000 moles.CO
2Collect in the scoop behind the sorbent material smoke outlet flue, recycle after the regeneration.
Claims (5)
1. system that utilizes flue gas of heating furnace to reclaim useless glycerine hydrogen manufacturing; It is characterized in that; Residual neat recovering system is installed in conventional hot rolling slab process furnace horizontal flue ingress; This system comprises aqueous glycerin solution preheater, projector, reactor drum and solid-gas separating device, with aqueous glycerin solution preheater and CO
2The parallel process furnace flue entrance top that is installed on of sorbent material preheater; The two is all placed perpendicular to horizontal direction; And link to each other with the projector that places flue entrance bottom (in the flue) through connecting tube respectively; The same with the projector flue that all places with solid-gas separating device of reactor drum is inner, and passes through connecting tube successively to connecting, and the modes of emplacement of the two all separates to guarantee solid-gas perpendicular to horizontal direction.
2. a kind of system that utilizes flue gas of heating furnace to reclaim useless glycerine hydrogen manufacturing according to claim 1 is characterized in that, above the projector of the flue outside, CO is installed
2Sorbent material adding set and CO
2The sorbent material preheating unit.
3. an application rights requires the 1 described recovery method that utilizes flue gas of heating furnace to reclaim useless glycerine hydrogen generating system, it is characterized in that,
A) at first solid-state discarded glycerine is collected, with the useless glycerine of collecting be mixed with glycerine and hydromassage you than the aqueous solution that is 1: 4～7, and this solution is heated to 65 ℃～75 ℃, filter removal impurity then and obtain pure aqueous glycerin solution;
B) this aqueous glycerin solution being added the mol ratio that is mixed with glycerine and water behind the water is 1: 8.9～9.3 aqueous solution, and pump carries out preheating to the glycerine preheater that places flue, simultaneously with CO
2Sorbent material imports to the preheater that places flue and carries out preheating from its adding set, both preheating temperature scopes are 510 ℃～530 ℃;
C) with aqueous glycerin solution after the preheating and CO
2Sorbent material imports in the projector, in projector, mixes, and feeds then in the reactor drum, and following reaction takes place in reactor drum:
C
3H
8O
3+3H
2O＝3CO
2+7H
2，ΔH
298＝128kJ/mol，
Temperature of reaction is 527 ℃～577 ℃, the CO in the resultant of reaction
2With CO
2Sorbent reactions, and add catalyzer, catalyst activity area＞70.00m2/g, the active time is 6～7 hours; The pressure condition of reaction is 1 normal atmosphere, and the flow velocity of aqueous glycerin solution is 0.4～0.7m/s, and the mass ratio of aqueous glycerin solution and sorbent material is 1: 3.1～3.3.
D) reactor drum is two groups, is used alternatingly resultant of reaction and CO
2Sorbent material relies on absorbent particles and gaseous mixture proportion different characteristic to realize that solid and gas separates in solid-gas separating device; Separate back gaseous product---hydrogen and water vapor; After removing water treatment, obtain clear energy sources hydrogen and be stored in the hydrogen cylinder the useless glycerine hydrogen production process of realization.
CO
2Sorbent material is collected in the sorbent material scoop after going out fly-ash separator, and sorbent material can be recycled through regeneration.
4. the recovery method that utilizes flue gas of heating furnace to reclaim useless glycerine hydrogen generating system according to claim 3 is characterized in that described CO
2Sorbent material is that particle diameter is the potassium activation Mg-Al based hydrotalcite of 38～180 μ m.
5. the recovery method that utilizes flue gas of heating furnace to reclaim useless glycerine hydrogen generating system according to claim 3 is characterized in that, described reaction institute catalyzer is a nickel, and used catalyzer is reusable through regenerating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110077814.1A CN102718184B (en) | 2011-03-29 | 2011-03-29 | System and method for recycling waste glycerol to produce hydrogen by using heating furnace flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110077814.1A CN102718184B (en) | 2011-03-29 | 2011-03-29 | System and method for recycling waste glycerol to produce hydrogen by using heating furnace flue gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102718184A true CN102718184A (en) | 2012-10-10 |
| CN102718184B CN102718184B (en) | 2015-04-08 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101062762A (en) * | 2007-05-10 | 2007-10-31 | 天津大学 | Method for producing synthetic gas by reforming by-product glycerin vapor of biological diesel production |
| CN101793466A (en) * | 2010-04-08 | 2010-08-04 | 张淑强 | Power-generating boiler capable of cooling steel products and recovering afterheat in steelmaking and steel-rolling process |
| CN101913561A (en) * | 2010-08-07 | 2010-12-15 | 大连理工大学 | Process for producing hydrogen by continuously catalyzing, absorbing, strengthening and reforming biological glycerine through moving bed |
-
2011
- 2011-03-29 CN CN201110077814.1A patent/CN102718184B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101062762A (en) * | 2007-05-10 | 2007-10-31 | 天津大学 | Method for producing synthetic gas by reforming by-product glycerin vapor of biological diesel production |
| CN101793466A (en) * | 2010-04-08 | 2010-08-04 | 张淑强 | Power-generating boiler capable of cooling steel products and recovering afterheat in steelmaking and steel-rolling process |
| CN101913561A (en) * | 2010-08-07 | 2010-12-15 | 大连理工大学 | Process for producing hydrogen by continuously catalyzing, absorbing, strengthening and reforming biological glycerine through moving bed |
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| CN102718184B (en) | 2015-04-08 |
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