CN103113190B - Butynediol low-pressure hydrogenation catalyst recycling process and system - Google Patents
Butynediol low-pressure hydrogenation catalyst recycling process and system Download PDFInfo
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- CN103113190B CN103113190B CN201310045482.8A CN201310045482A CN103113190B CN 103113190 B CN103113190 B CN 103113190B CN 201310045482 A CN201310045482 A CN 201310045482A CN 103113190 B CN103113190 B CN 103113190B
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- catalyst
- butynediol
- isosorbide
- catalyzer
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- 239000003054 catalyst Substances 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 35
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 30
- 238000004064 recycling Methods 0.000 title abstract 3
- 239000002002 slurry Substances 0.000 claims abstract description 44
- 238000011084 recovery Methods 0.000 claims abstract description 17
- 238000007701 flash-distillation Methods 0.000 claims abstract description 6
- CDQSJQSWAWPGKG-UHFFFAOYSA-N butane-1,1-diol Chemical compound CCCC(O)O CDQSJQSWAWPGKG-UHFFFAOYSA-N 0.000 claims description 20
- 239000002562 thickening agent Substances 0.000 claims description 19
- PUPZLCDOIYMWBV-UHFFFAOYSA-N (+/-)-1,3-Butanediol Chemical compound CC(O)CCO PUPZLCDOIYMWBV-UHFFFAOYSA-N 0.000 claims description 12
- -1 butyne diol Chemical class 0.000 claims description 12
- 239000001257 hydrogen Substances 0.000 claims description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 10
- 210000002966 serum Anatomy 0.000 claims description 10
- KDKYADYSIPSCCQ-UHFFFAOYSA-N ethyl acetylene Natural products CCC#C KDKYADYSIPSCCQ-UHFFFAOYSA-N 0.000 claims description 9
- 239000008187 granular material Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000001914 filtration Methods 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000007670 refining Methods 0.000 abstract 2
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 239000007788 liquid Substances 0.000 abstract 1
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- 239000005997 Calcium carbide Substances 0.000 description 2
- XXROGKLTLUQVRX-UHFFFAOYSA-N allyl alcohol Chemical compound OCC=C XXROGKLTLUQVRX-UHFFFAOYSA-N 0.000 description 2
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 2
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 description 2
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Heterocyclic Carbon Compounds Containing A Hetero Ring Having Oxygen Or Sulfur (AREA)
Abstract
The invention relates to a butynediol low-pressure hydrogenation catalyst recycling process and system, and solves the problems that multiple butynediol low-pressure hydrogenation catalyst recycling apparatuses exist, the filtration efficiency is low, the catalyst recovery rate is low, the process period is long, the energy consumption is high and the operating cost is high in the prior art. According to the technical scheme, the system comprises a slurry trough, a slurry pump and a hydrogenation reactor which are sequentially connected through pipelines, and is sequentially connected with a gas-liquid separation tank, a concentrator and a refining filter. The process comprises the following steps: performing hydrogenation reaction on a butynediol solution, performing flash distillation, concentrating, refining to obtain a 1,4-butanediol solution, and recovering the catalyst. The system provided by the invention is simple and low in investment and operating cost; and the process provided by the invention greatly reduces the number of apparatuses for catalyst recovery, realizes the high-efficiency recovery and cyclic utilization of the butynediol low-pressure hydrogenation catalyst and has high environmental protection and economic values.
Description
Technical field
The present invention relates to the synthetic preparation field of a kind of Isosorbide-5-Nitrae butyleneglycol, a kind of butynediol low-voltage hydrogenation catalyst recovery is utilized technique and system specifically.
Background technology
BDO is a kind of important basic organic chemical industry raw material and fine chemical material, of many uses, and at present, the Isosorbide-5-Nitrae butyleneglycol production technique in the whole world mainly comprises alkynes aldehyde method, butadiene process, butane/cis-butenedioic anhydride method, propylene oxide/vinylcarbinol method.The technique of using from worldwide production business, alkynes aldehyde method technique production capacity share accounts for larger advantage.
The main raw material that alkynes aldehyde method (Reppe method) is produced BDO has calcium carbide, methyl alcohol and hydrogen.Wherein, calcium carbide is mainly used to prepare acetylene, and methyl alcohol is used for preparing formaldehyde.Acetylene and formaldehyde are prepared butynediol by ethynylation.Butynediol can be prepared BDO by low-voltage hydrogenation and high-pressure hydrogenation reaction process.
Because butynediol low-voltage hydrogenation process is carried out in Gas-Liuid-Solid three phases reactor, after having reacted, hydrogen, catalyzer and BDO product solution need separated.In traditional technology route, from the low pressure Isosorbide-5-Nitrae butanediol solution of low-voltage hydrogenation reactor and the mixed serum of catalyzer, enter subsider, isolate the slurries that contain granules of catalyst.Granules of catalyst is deposited to subsider bottom, then with pump, is sent back to slurry tank, by pump, again squeezes into low-voltage hydrogenation reactor again.Isosorbide-5-Nitrae butyleneglycol product, by the weir on subsider top, overflows to product groove.Principle due to subsider employing gravity settling separation, only for granules of catalyst more than 30 μ m, there is separating effect, for short grained catalyzer, be difficult to realize separated, therefore by subsider top, overflowed 1, therefore still the catalyzer that contains more small particle size in 4 butyleneglycol products, must be after pump pressurization further through heavy filtrations of a plurality of equipment such as electromagnetic filter, disk filter, fine filter I and fine filter II successively separatedly just can enter subsequent processing after removing granules of catalyst.
There is the problem that filter plant is numerous, filtration efficiency is low, catalyst recovery yield is low, process cycle is long, energy consumption is high, running cost is high in current technical process.
Summary of the invention
To the object of the invention is in order solving the problems of the technologies described above, to provide that a kind of technique is simple, the cycle is short, energy consumption is low, catalyst recovery yield is high, facility investment and the low butynediol low-voltage hydrogenation catalyst recovery of running cost utilize technique.
The present invention also provides a kind of system for above-mentioned technique.
System of the present invention comprises slurry tank, slush pump and the hydrogenator connecting successively through pipeline, is also connected with knockout drum, thickener and fine filter in turn.
Described thickener comprises slurries outlet and taphole, and described slurries outlet is connected with slurry tank through pipeline, and described taphole is connected with fine filter.
Butynediol low-voltage hydrogenation catalyst recovery of the present invention is utilized technique, comprises the following steps:
(1). the mixed serum of butyne diol solutions and catalyst slurry is sent in hydrogenator through slush pump in slurry tank, in hydrogenator, butynediol under catalyst action with H
2reaction generates Isosorbide-5-Nitrae butyleneglycol, obtains the Isosorbide-5-Nitrae butanediol solution that contains catalyzer and hydrogen;
(2). the Isosorbide-5-Nitrae butyleneglycol product solution that contains catalyzer and hydrogen generating through hydrogenator, first enters knockout drum and flashes off the H being dissolved in liquid phase
2, obtain the Isosorbide-5-Nitrae butanediol solution that contains catalyzer;
(3). it is concentrated that the Isosorbide-5-Nitrae butanediol solution that contains catalyzer obtaining after flash distillation enters thickener again, isolates the catalyst slurry and the Isosorbide-5-Nitrae butanediol solution that contain granules of catalyst more than 10 μ m after thickener;
(4). described after thickener the Isosorbide-5-Nitrae butanediol solution of isolated catalyst content≤15ppm after fine filter filters, send into subsequent processing.
The catalyst slurry that described step (3) obtains is back to slurry tank and butyne diol solutions is mixed to get mixed serum, more again enters low-voltage hydrogenation reactor through slush pump pressurization.
The catalyst content of controlling in the Isosorbide-5-Nitrae butanediol solution that contains catalyzer after flash distillation in described step (2) is 3-7wt%.
Controlling the catalyst content in catalyst slurry described in described step (3) is 9-12 wt %.
It is 0.10-0.15 that control enters before hydrogenator the mass ratio of catalyzer and butynediol in mixed serum, while going into operation, can be first butyne diol solutions be sent into back to hydrogen reactor again with after fresh catalyst slurry mixes in slurry tank, when system is normally moved, the catalyst slurry being drawn back by thickener is directly mixed with butyne diol solutions, in operational process, detect in real time the content ratio of catalyzer and butynediol, to meet the requirement of follow-up hydrogenation reaction, when detect catalyzer when the quantity not sufficient, can in slurry tank, supplement appropriate catalyzer to make up the loss amount in catalyst recovery process.
Described catalyzer is nickel-base catalyst conventional in butynediol hydrogenation reaction, can enumerate and not limit the A-7063 type catalyzer produced as the Johnson mapphey company of Britain etc., and described catalyst slurry comprises evenly outstanding mixed catalyzer and water.Described butyne diol solutions is from existing ethynylation unit.In technique of the present invention, at hydrogenator reacted 1, in 4 butanediol solutions, contain hydrogen and catalyzer, first utilize knockout drum that hydrogen is flashed off, and then by thickener to containing 1 of catalyzer, 4 butanediol solutions concentrate, this concentration process is compared with the process of the gravity settling separation in past, have the following advantages: (2) good separating effect, can disposable the catalyst slurry that contains the above granules of catalyst of 10 μ m be separated, by once concentration, just can guarantee to obtain 1, be down to≤15ppm(of catalyst content in 4 butanediol solutions mass percent), thereby follow-up need be carried out primary purification and filter and just can meet the demand of subsequent processing in a fine filter, thereby the required various filter plants of follow-up multiple times of filtration have been greatly reduced, greatly reduce the investment of equipment and the energy consumption of bringing thus, shortened process cycle.(2), because enrichment step is low voltage operated, the catalyst slurry therefore obtaining can pressurize without pump, utilizes the pressure of self can be back to slurry tank, thereby has reduced the energy consumption of pump.(3) because most of catalyzer is separated in thickener, thereby greatly improve the rate of recovery of catalyzer, reduced the loss of catalyzer, be conducive to further reduce running cost.
System of the present invention is simple, and investment and running cost are low, and technique of the present invention has significantly been reduced the required number of devices of catalyst recovery, has realized the high efficiente callback recycle of butynediol low-voltage hydrogenation catalyzer, has very high environmental protection and economic worth.
Accompanying drawing explanation
Fig. 1 is system schematic of the present invention and mechanical flow digram.
Wherein, 1-slurry tank, 2-slush pump, 3-low-voltage hydrogenation reactor, 4-flash drum, 5-thickener, the outlet of 5.1-slurries, 5.2-taphole, 6-fine filter.
Embodiment
System embodiment:
With reference to Fig. 1, slurry tank 1 is connected by pipeline with low-voltage hydrogenation reactor 3, knockout drum 4, thickener 5 and fine filter 6 successively through slush pump 2, wherein, described thickener comprises slurries outlet 5.1 and taphole 5.2, described slurries outlet 5.1 is connected with slurry tank 1 through pipeline, and described taphole 5.2 is connected with fine filter 6.
Process example:
With reference to Fig. 1,
(1). the mixed serum of the interior butyne diol solutions of slurry tank 1 and catalyst slurry (in mixed serum, the mass ratio of catalyzer and butynediol is 0.10-0.15) is sent in low-voltage hydrogenation reactor through slush pump 2, in low-voltage hydrogenation reactor 3 butynediol under catalyst action with H
2reaction generates Isosorbide-5-Nitrae butyleneglycol, obtains the Isosorbide-5-Nitrae butanediol solution that contains catalyzer and hydrogen;
(2). the Isosorbide-5-Nitrae butyleneglycol product solution that contains catalyzer and hydrogen generating through hydrogenator 3, first enters knockout drum 4 and flashes off the H being dissolved in liquid phase
2, obtain the Isosorbide-5-Nitrae butanediol solution (catalyst content is 3-7wt%) that contains catalyzer;
(3). what after flash distillation, obtain contains 1 of catalyzer, it is concentrated that 4 butanediol solutions enter thickener 5 again, after thickener, isolate the catalyst slurry (catalyst content is 9-12 wt %) and the Isosorbide-5-Nitrae butanediol solution that contain granules of catalyst more than 10 μ m;
(4). described after thickener 5 the Isosorbide-5-Nitrae butanediol solution of isolated catalyst content≤15ppm by taphole 5.2, discharged to send into after fine filter 6 filters and send into subsequent processing; Described step (3) obtains catalyst slurry and through slurries outlet 5.1, is back in slurry tank 1 and is mixed to get mixed serum with butyne diol solutions under low pressure effect, more again enters low-voltage hydrogenation reactor 3 through slush pump 2 pressurizations.
Take that to produce 50000 tons of Isosorbide-5-Nitrae butyleneglycol projects per year be example, the application of system of the present invention, can save facility investment 2,600 ten thousand every year, reduces energy consumption 60,000 kwh/, and catalyzer more than 10um is recycled substantially.
Claims (5)
1. a butynediol low-voltage hydrogenation catalyst recovery is utilized system, comprise the slurry tank, slush pump and the hydrogenator that through pipeline, connect successively, it is characterized in that, also be connected with knockout drum, thickener and fine filter in turn, described thickener comprises slurries outlet and taphole, described slurries outlet is connected with slurry tank through pipeline, and described taphole is connected with fine filter.
2. butynediol low-voltage hydrogenation catalyst recovery is utilized a technique, it is characterized in that, comprises the following steps:
(1). the mixed serum of butyne diol solutions and catalyst slurry is sent in hydrogenator through slush pump in slurry tank, in hydrogenator, butynediol under catalyst action with H
2reaction generates Isosorbide-5-Nitrae butyleneglycol, obtains the Isosorbide-5-Nitrae butanediol solution that contains catalyzer and hydrogen;
(2). the Isosorbide-5-Nitrae butyleneglycol product solution that contains catalyzer and hydrogen generating through hydrogenator, first enter knockout drum and flash off the H2 being dissolved in liquid phase, obtain the Isosorbide-5-Nitrae butanediol solution that contains catalyzer;
(3). what after flash distillation, obtain contains 1 of catalyzer, it is concentrated that 4 butanediol solutions enter thickener again, after thickener, isolate the catalyst slurry and 1 that contains granules of catalyst more than 10 μ m, 4 butyleneglycol product solutions, the catalyst slurry obtaining is back to slurry tank and butyne diol solutions is mixed to get mixed serum, more again enters low-voltage hydrogenation reactor through slush pump pressurization;
(4). described after thickener the Isosorbide-5-Nitrae butanediol solution of isolated catalyst content≤15ppm after fine filter filters, send into subsequent processing.
3. butynediol low-voltage hydrogenation catalyst recovery as claimed in claim 2 is utilized technique, it is characterized in that, the catalyst content of controlling in the Isosorbide-5-Nitrae butanediol solution that contains catalyzer after flash distillation in described step (2) is 3-7wt%.
4. butynediol low-voltage hydrogenation catalyst recovery as claimed in claim 2 is utilized technique, it is characterized in that, controlling the catalyst content in catalyst slurry described in described step (3) is 9-12wt%.
5. butynediol low-voltage hydrogenation catalyst recovery as claimed in claim 2 is utilized technique, it is characterized in that, controlling and entering before hydrogenator the mass ratio of catalyzer and butynediol in mixed serum is 0.10-0.15.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310045482.8A CN103113190B (en) | 2013-02-05 | 2013-02-05 | Butynediol low-pressure hydrogenation catalyst recycling process and system |
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| CN201310045482.8A CN103113190B (en) | 2013-02-05 | 2013-02-05 | Butynediol low-pressure hydrogenation catalyst recycling process and system |
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| CN103113190A CN103113190A (en) | 2013-05-22 |
| CN103113190B true CN103113190B (en) | 2014-12-03 |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106815497B (en) | 2015-12-01 | 2019-04-23 | 华为终端（东莞）有限公司 | An interface processing method, electronic device and graphical user interface |
| CN106928022B (en) * | 2017-02-28 | 2020-04-28 | 苏英慧 | Method for controlling sedimentation distribution of nickel in butynediol solution |
| CN107141196A (en) * | 2017-06-27 | 2017-09-08 | 查都（上海）科技有限公司 | A kind of 1,4 butynediols two-stage hydrogenation systems |
| CN107541345B (en) * | 2017-10-31 | 2020-06-26 | 南通市康桥油脂有限公司 | A kind of recovery process of stearic acid hydrogenation catalyst |
| CN118663167B (en) * | 2023-03-16 | 2025-11-14 | 中国石油化工股份有限公司 | System and method for producing 1,4-butanediol by hydrogenation of 1,4-butynediol |
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| US4213000A (en) * | 1979-05-29 | 1980-07-15 | E. I. Du Pont De Nemours And Company | Reducing color formers in 1,4-butanediol |
| CN1222902A (en) * | 1996-10-10 | 1999-07-14 | 巴斯福股份公司 | Method for preparing 1,4-butanediol by catalytic hydrogenation of 1,4-butynediol |
| CN102658213A (en) * | 2012-05-04 | 2012-09-12 | 上海华畅环保设备发展有限公司 | Method and device for concentrating and coupled-drying catalyst in quenched wastewater in process of using methanol to prepare olefin |
| CN203187603U (en) * | 2013-02-05 | 2013-09-11 | 中国五环工程有限公司 | System for recycling butynediol low-pressure hydrogenation catalyst |
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2013
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| US4213000A (en) * | 1979-05-29 | 1980-07-15 | E. I. Du Pont De Nemours And Company | Reducing color formers in 1,4-butanediol |
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