CN103819298B - C-2-fraction selective hydrogenation method - Google Patents
C-2-fraction selective hydrogenation method Download PDFInfo
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- CN103819298B CN103819298B CN201410084384.XA CN201410084384A CN103819298B CN 103819298 B CN103819298 B CN 103819298B CN 201410084384 A CN201410084384 A CN 201410084384A CN 103819298 B CN103819298 B CN 103819298B
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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
- Y02P20/584—Recycling of catalysts
Abstract
The present invention relates to a kind of C-2-fraction selective hydrogenation method, mainly to solve in prior art reactor size compared with the problem large, loaded catalyst is many, resurgent gases consumption is large.The present invention is by adopting a kind of C-2-fraction selective hydrogenation method, the C-2-fraction of acetylene volumetric molar concentration≤15000ppm and hydrogen enter wherein at least two fixed-bed reactor in the reactive system comprising at least three fixed-bed reactor in parallel, contact with selective hydrogenation catalyst, obtain the C-2-fraction of acetylene volumetric molar concentration≤1ppm, remaining fixed-bed reactor are used for technical scheme for subsequent use or catalyst regeneration and solve the problems referred to above preferably, can be used in C-2-fraction hydrogenation.
Description
Technical field
The present invention relates to a kind of C-2-fraction selective hydrogenation method.
Background technology
At present, no matter be large-scale ethylene plant, or large-scale methanol-to-olefins (MTO) device, its reaction generates removing of acetylene in gas, when not needing to reclaim acetylene, generally adopts shortening method.Make spent hydroprocessing catalyst, under certain processing condition, acetylene hydrogenation generates corresponding carbon diolefine, thus reaches the object removing acetylene.
CN200910092084.5 relates to a kind of C 2 fraction selective hydrogenation method, and employing carrier is Al
2o
3pd and Ag catalyst removal C-2-fraction in acetylene.After carbon two selective hydrogenation catalyst uses certain hour, its selectivity declines and is difficult to maintain normal running, needs to recover its activity by manipulation of regeneration.CN01139822.1 relates to the ex-situ regeneration technique of hydrogenation catalyst, describes the outer high temperature of the catalyst device used in a kind of oil refinery and burns process process engineering for regenerating.CN201110027356 relates to a kind of renovation process of novel hydrogenation catalyzer, is a kind of method of the ex-situ regeneration of hydrogenation catalyst that conventional coke burning regeneration and chemistry are combined.
In prior art, the technical process that ethylene unit and MTO device C 2 fraction selective hydrogenation and catalyst regeneration flow process adopt " one open one standby ", one for hydrogenation reaction, another is for regeneration or for subsequent use, the loadings of every platform hydrogenator catalyzer is 100%, in regenerative process, needs the resurgent gases of consumption 100%, there is catalyst for hydrogenation loadings many, the problems such as resurgent gases consumption is large.
The present invention solves the problems referred to above targetedly.
Summary of the invention
Technical problem to be solved by this invention is that in prior art, reactor size, compared with the problem large, loaded catalyst is many, resurgent gases consumption is large, provides a kind of new C-2-fraction selective hydrogenation method.This technique is used for, in C-2-fraction hydrogenation, having reactor size compared with little, that loaded catalyst is few, resurgent gases consumption is little advantage.
For solving the problem, the technical solution used in the present invention is as follows: a kind of C-2-fraction selective hydrogenation method, the C-2-fraction of acetylene volumetric molar concentration≤15000ppm and hydrogen enter wherein at least two fixed-bed reactor in the reactive system comprising at least three fixed-bed reactor in parallel, contact with selective hydrogenation catalyst, obtain the C-2-fraction of acetylene volumetric molar concentration≤1ppm, remaining fixed-bed reactor are used for for subsequent use or catalyst regeneration.
In technique scheme, preferably, in described selective hydrogenation catalyst, active ingredient comprises Pd and Ag, and carrier is Al
2o
3.
In technique scheme, preferably, described C-2-fraction and hydrogen enter wherein two fixed-bed reactor in the reactive system of three fixed-bed reactor in parallel, another fixed-bed reactor are used for regeneration, working pressure for two fixed-bed reactor of hydrogenation is 1.00 ~ 3.00MPaG, service temperature is 20 ~ 150 DEG C, and the gas volume air speed in every platform fixed-bed reactor is 3000 ~ 6000h
-1.
In technique scheme, more preferably, the working pressure of described two fixed-bed reactor for hydrogenation is 1.55 ~ 2.55MPaG, and service temperature is 30 ~ 100 DEG C.
In technique scheme, most preferably, the working pressure of described two fixed-bed reactor for hydrogenation is 1.85 ~ 2.05MPaG, and service temperature is 40 ~ 80 DEG C.
In technique scheme, preferably, when remaining fixed-bed reactor are used for catalyst regeneration, working pressure is 0.4 ~ 1.4MPaG, and service temperature is 90 ~ 510 DEG C, gas space velocity 200h
-1.
In technique scheme, more preferably, when remaining fixed-bed reactor are used for catalyst regeneration, working pressure is 0.6 ~ 1.0MPaG, and service temperature is 100 ~ 510 DEG C.
In technique scheme, preferably, described fixed-bed reactor inner catalyst bed at least two sections, intersegmentally arranges interchanger.
The technical process that the technical process of " open standby " of prior art is improved at least by the present invention " two open one standby ", separate unit reactor size is reduced, loaded catalyst declines 25%, and resurgent gases consumption is corresponding reduction by 50% also, achieves good technique effect.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
The one that the present invention relates to energy-saving low-carbon alkene tripping device carbon two selective hydrogenation reclaiming process is 300,000 tons/year of ethylene units for the production of scale.Reactive system comprises three fixed-bed reactor, and C-2-fraction and hydrogen enter wherein two, and another is for catalyst regeneration.In C 2 fraction selective hydrogenation catalysts, active ingredient is Pd and Ag, and carrier is Al
2o
3, model is that the massfraction of BC-1-037, load P d and Ag is respectively 0.03%, 0.20%.Acetylene volumetric molar concentration≤15000ppm contained by the C-2-fraction of hydrogenator import, acetylene volumetric molar concentration < 1ppm contained by the C-2-fraction of hydrogenator outlet; Hydrogenation fixed-bed reactor inner catalyst bed is two sections, intersegmentally arranges interchanger.Hydrogenation operation pressure is 1.00MPaG, and initial stage service temperature is 20 DEG C, and final service temperature is 80 DEG C, gas space velocity 3000h
-1; Catalyst regeneration working pressure is 0.4MPaG, and initial stage service temperature is 90 DEG C, and maximum operating temperature is 510 DEG C, and resurgent gases volume space velocity is 200h
-1.Every platform hydrogenator is of a size of Ф 3000 × 4820mm, and three reactor catalyst loadings are 71.5m
3, regeneration nitrogen flow is 10000kg/h.
[embodiment 2]
According to condition and the step of embodiment 1, in C 2 fraction selective hydrogenation catalysts, active ingredient is Pd and Ag, and carrier is Al
2o
3, model is that the massfraction of BC-H-20A, load P d and Ag is respectively 0.04%, 0.12%.Acetylene volumetric molar concentration≤15000ppm contained by the C-2-fraction of hydrogenator import, acetylene volumetric molar concentration < 1ppm contained by the C-2-fraction of hydrogenator outlet; Hydrogenation operation pressure is 3.00MPaG, and initial stage service temperature is 40 DEG C, and final service temperature is 150 DEG C, gas volume air speed 6000h
-1; Catalyst regeneration working pressure is 1.4MPaG, and initial stage service temperature is 100 DEG C, and maximum operating temperature is 510 DEG C, and resurgent gases volume space velocity is 200h
-1.Every platform hydrogenator is of a size of Ф 3600 × 5000mm, and the loaded catalyst of three reactors is 107m
3, regeneration nitrogen flow is 12000kg/h.
[embodiment 3]
The one that the present invention relates to energy-saving low-carbon alkene tripping device carbon two selective hydrogenation reclaiming process is 600,000 tons/year of MTO devices for the production of scale.Reactive system comprises three fixed-bed reactor, and C-2-fraction and hydrogen enter wherein two, and another is for catalyst regeneration.In C 2 fraction selective hydrogenation catalysts, active ingredient is Pd and Ag, and carrier is Al
2o
3, model is that the massfraction of BC-1-037A, load P d and Ag is respectively 0.05%, 0.05%.Acetylene volumetric molar concentration≤15000ppm contained by the C-2-fraction of hydrogenator import, acetylene volumetric molar concentration < 1ppm contained by the C-2-fraction of hydrogenator outlet; Hydrogenation operation pressure is 1.90MPaG, and initial stage service temperature is 30 DEG C, and final service temperature is 80 DEG C, gas volume air speed 4000h
-1; Catalyst regeneration working pressure is 0.8MPaG, and initial stage service temperature is 100 DEG C, and maximum operating temperature is 510 DEG C, and resurgent gases volume space velocity is 200h
-1.Every platform hydrogenator size Ф 1600 × 3340mm, the loaded catalyst of three reactors is 14.1m
3, regeneration nitrogen flow is 9000kg/h.
[comparative example 1]
According to the condition described in embodiment 1, adopt " one open one standby " technique of prior art, acetylene volumetric molar concentration≤15000ppm contained by the C-2-fraction of hydrogenator import, acetylene volumetric molar concentration < 1ppm contained by the C-2-fraction of hydrogenator outlet; Every platform hydrogenator size Ф 3800 × 6000mm, the loaded catalyst of three reactors is 95.2m
3, regeneration nitrogen flow is 20000kg/h.
[comparative example 2]
According to the condition described in embodiment 2, adopt " one open one standby " technique of prior art, acetylene volumetric molar concentration≤15000ppm contained by the C-2-fraction of hydrogenator import, acetylene volumetric molar concentration < 1ppm contained by the C-2-fraction of hydrogenator outlet; Every platform hydrogenator size Ф 4400 × 6700mm, the loaded catalyst of three reactors is 143m
3, regeneration nitrogen flow is 24000kg/h.
[comparative example 3]
According to the condition described in embodiment 3, adopt " one open one standby " technique of prior art, acetylene volumetric molar concentration≤15000ppm contained by the C-2-fraction of hydrogenator import, acetylene volumetric molar concentration < 1ppm contained by the C-2-fraction of hydrogenator outlet; Every platform hydrogenator size Ф 2000 × 4300mm, the loaded catalyst of three reactors is 18.9m
3, regeneration nitrogen flow is 18000kg/h.
Claims (7)
1. a C-2-fraction selective hydrogenation method, the C-2-fraction of acetylene volumetric molar concentration≤15000ppm and hydrogen enter wherein at least two fixed-bed reactor in the reactive system comprising at least three fixed-bed reactor in parallel, contact with selective hydrogenation catalyst, obtain the C-2-fraction of acetylene volumetric molar concentration≤1ppm, remaining fixed-bed reactor are used for for subsequent use or catalyst regeneration; Described fixed-bed reactor inner catalyst bed at least two sections, intersegmentally arranges interchanger.
2. C-2-fraction selective hydrogenation method according to claim 1, it is characterized in that in described selective hydrogenation catalyst, active ingredient comprises Pd and Ag, carrier is Al
2o
3.
3. C-2-fraction selective hydrogenation method according to claim 1, it is characterized in that described C-2-fraction and hydrogen enter wherein two fixed-bed reactor in the reactive system of three fixed-bed reactor in parallel, another fixed-bed reactor are used for regeneration, working pressure for two fixed-bed reactor of hydrogenation is 1.00 ~ 3.00MPaG, service temperature is 20 ~ 150 DEG C, and the gas volume air speed in every platform fixed-bed reactor is 3000 ~ 6000h
-1.
4. C-2-fraction selective hydrogenation method according to claim 3, it is characterized in that the described working pressure for two fixed-bed reactor of hydrogenation is 1.55 ~ 2.55MPaG, service temperature is 30 ~ 100 DEG C.
5. C-2-fraction selective hydrogenation method according to claim 4, it is characterized in that the described working pressure for two fixed-bed reactor of hydrogenation is 1.85 ~ 2.05MPaG, service temperature is 40 ~ 80 DEG C.
6. C-2-fraction selective hydrogenation method according to claim 1, is characterized in that working pressure is 0.4 ~ 1.4MPaG, and service temperature is 90 ~ 510 DEG C, gas space velocity 200h when remaining fixed-bed reactor are for catalyst regeneration
-1.
7. C-2-fraction selective hydrogenation method according to claim 6, is characterized in that working pressure is 0.6 ~ 1.0MPaG, and service temperature is 100 ~ 510 DEG C when remaining fixed-bed reactor are for catalyst regeneration.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0334742A1 (en) * | 1988-03-23 | 1989-09-27 | Institut Français du Pétrole | Liquid phase selective hydrogenation of a normally gaseous feedstock containing ethylene, acetylene and naptha |
| US5763715A (en) * | 1996-10-08 | 1998-06-09 | Stone & Webster Engineering Corp. | Butadiene removal system for ethylene plants with front end hydrogenation systems |
| CN101913975A (en) * | 2009-09-15 | 2010-12-15 | 中国石油天然气股份有限公司 | Selective hydrogenation method for C2 distillate |
| CN102060647A (en) * | 2010-12-03 | 2011-05-18 | 中国石油天然气股份有限公司 | Selective hydrogenation method of C-2-fraction |
-
2014
- 2014-03-07 CN CN201410084384.XA patent/CN103819298B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0334742A1 (en) * | 1988-03-23 | 1989-09-27 | Institut Français du Pétrole | Liquid phase selective hydrogenation of a normally gaseous feedstock containing ethylene, acetylene and naptha |
| US5763715A (en) * | 1996-10-08 | 1998-06-09 | Stone & Webster Engineering Corp. | Butadiene removal system for ethylene plants with front end hydrogenation systems |
| CN101913975A (en) * | 2009-09-15 | 2010-12-15 | 中国石油天然气股份有限公司 | Selective hydrogenation method for C2 distillate |
| CN102060647A (en) * | 2010-12-03 | 2011-05-18 | 中国石油天然气股份有限公司 | Selective hydrogenation method of C-2-fraction |
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