CN106753818A - The hydrogenation apparatus and heat of reaction recovery method of a kind of recyclable heat of reaction - Google Patents
The hydrogenation apparatus and heat of reaction recovery method of a kind of recyclable heat of reaction Download PDFInfo
- Publication number
- CN106753818A CN106753818A CN201611245885.7A CN201611245885A CN106753818A CN 106753818 A CN106753818 A CN 106753818A CN 201611245885 A CN201611245885 A CN 201611245885A CN 106753818 A CN106753818 A CN 106753818A
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- China
- Prior art keywords
- hydrogenation
- heat
- steam generator
- pneumatic
- reactor
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 91
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 12
- 238000011084 recovery Methods 0.000 title claims abstract description 12
- 239000008234 soft water Substances 0.000 claims abstract description 23
- 239000000203 mixture Substances 0.000 claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 13
- 238000007599 discharging Methods 0.000 claims abstract description 5
- 238000001816 cooling Methods 0.000 claims abstract description 3
- 239000003054 catalyst Substances 0.000 claims description 7
- 239000001257 hydrogen Substances 0.000 claims description 7
- 229910052739 hydrogen Inorganic materials 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 7
- 239000002253 acid Substances 0.000 claims description 6
- 239000004519 grease Substances 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 125000001931 aliphatic group Chemical group 0.000 claims description 5
- 239000007789 gas Substances 0.000 claims 1
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 description 6
- 229910052740 iodine Inorganic materials 0.000 description 6
- 239000011630 iodine Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 235000014113 dietary fatty acids Nutrition 0.000 description 3
- 229930195729 fatty acid Natural products 0.000 description 3
- 239000000194 fatty acid Substances 0.000 description 3
- 150000004665 fatty acids Chemical class 0.000 description 3
- 238000010025 steaming Methods 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- -1 aliphatic acid Chemical class 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/12—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by hydrogenation
Landscapes
- Chemical & Material Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to the hydrogenation apparatus and heat of reaction recovery method of a kind of recyclable heat of reaction.Can disposably hydrogenation be in place in the device hydrogenation process that purpose is to provide.Technical scheme is：A kind of hydrogenation apparatus of recyclable heat of reaction, including it is provided with the hydrogenation tower of hydrogenation oil export；The device accesses the mixture inlet of hydrogenation tower entrance, hydrogenation pre-reactor and steam generator again after being also sequentially connected using pipeline.A kind of recovery method of hydrogenation heat, follows the steps below：1) in mixture input hydrogenation pre-reactor, preliminary hydrogenation is carried out in pre-reactor is hydrogenated；2) material of hydrogenation pre-reactor outlet output enters steam generator, and heat exchange is carried out with soft water, and hydrogenation is proceeded in after steam generator heat exchange cooling, entering back into hydrogenation tower；Then discharging exports finished product；3) soft water enters steam generator, absorbs the steam produced after heat and is incorporated to plant area's steam pipe system.
Description
Technical field
The invention belongs to oil and fat chemical production field, more particularly to a kind of hydrogenation apparatus of recyclable heat of reaction
And heat of reaction recovery method.
Technical background
In the production of grease (or aliphatic acid) hydrogenation, grease (or aliphatic acid) and hydrogen occur under catalyst action
Hydrogenation obtains hydrogenated oil and fat (or hydrogenated fatty acid)；Hydrogenation is exothermic reaction, and general raw oil material (or aliphatic acid) is every
1 iodine number of unit is reduced, temperature of charge can raise 1.6-1.7 DEG C；Current domestic manufacturer uses single hydrogenation tower
Hydrogenation is carried out, if the iodine number of raw material is higher, the temperature of charge in hydrogenation tower can raise more, design and pipeline to tower
The requirement of valve is higher, and security risk is higher.In addition, high temperature can also influence the quality of product, product color to deepen, accessory substance increases
Many, to avoid overtemperature, typically using multiple hydrogenation, such production efficiency is substantially reduced, and energy consumption doubles the above.
The content of the invention
The purpose of the present invention is to overcome the shortcomings of above-mentioned background technology, there is provided a kind of recovery of recyclable hydrogenation heat
Device and corresponding hydrogenation heat recovery method, disposably can arrive hydrogenation in the device hydrogenation process
Position, can produce steam, reduce production energy resource consumption, while temperature can be effectively controlled in production process, product quality
It is guaranteed.
The present invention provide technical scheme be：
A kind of hydrogenation apparatus of recyclable heat of reaction, including it is provided with the hydrogenation tower of hydrogenation oil export；Its feature exists
Accessed again after the device is also sequentially connected using pipeline hydrogenation tower entrance mixture inlet, hydrogenation pre-reactor and
Steam generator；
The hydrogenation pre-reactor first half is provided with highly different multiple outlets, and these outlets are by each communicating with and band
Steam generator is connected again after having the pipeline parallel connection of pneumatic on-off valve, it is different with the temperature according to hydrogenation pre-reactor outlet material
It is separately turned on；
The steam output of the soft water input pipe and output steam of input soft water is connected with the steam generator
Pipe.
The first pneumatic control valve is provided with the soft water pipeline, the pneumatic control valve is carried out with the liquid level gauge of steam generator
Chain control；The second pneumatic control valve is provided with the jet chimney, the pneumatic control valve is passed with the pressure on steam generator
Sensor carries out chain control.
The mixture is grease or aliphatic acid, the mixing with hydrogen and catalyst.
It is described to hydrogenate pre-reactor with steam generator to cover series system more.
A kind of recovery method of hydrogenation heat, follows the steps below：
1) in mixture input hydrogenation pre-reactor, preliminary hydrogenation is carried out in pre-reactor is hydrogenated；The hydrogenation
Pre-reactor outlet mass temperatures are controlled at 180-230 DEG C；
2) material of hydrogenation pre-reactor outlet output enters steam generator, heat exchange is carried out with soft water, by steaming
Vapour generator heat exchange cooling after, enter back into hydrogenation tower in proceed hydrogenation；Then discharging exports finished product；
3) soft water enters steam generator, absorbs the steam produced after heat and is incorporated to plant area's steam pipe system.
Step 1) in, the outlet mass temperatures of pre-reactor are hydrogenated, by adjusting the first pneumatic on-off valve, second pneumatic opening
The different opening for closing valve and the 3rd pneumatic on-off valve is controlled.
Step 3) in, the reaction temperature section in hydrogenation tower, by the first pneumatic on-off valve, the second pneumatic on-off valve and the
Three pneumatic on-off valves be turned on and off realize.
The present invention compared with prior art, with advantage following prominent and good effect：
1st, the device and technological process for being provided using the present invention can be recycled to the heat in hydrogenation reaction, be dropped
Low more than 80% energy resource consumption；
2nd, temperature is effectively controlled in production process, and product quality is effectively ensured, and also eliminating overtemperature production can
The potential safety hazard that can be brought.
Brief description of the drawings
Fig. 1 is the structural representation of hydrogenation heat reclaim unit of the present invention.
In figure, 1 is mixture inlet；2nd, it is hydrogenation pre-reactor；3 is the first pneumatic on-off valve；4 is the second jettron
Valve；5 is the 3rd pneumatic on-off valve；6 is steam generator；7 is the first pneumatic control valve；8 is soft water；9 is the second pneumatic regulation
Valve；10 is the steam for removing plant area's pipe network；11 is hydrogenation tower；12 is finished product (hydrogenated oil and fat or hydrogenated fatty acid)；T is thermometer.
Specific embodiment
Further illustrated below in conjunction with embodiment shown in the drawings.
The retracting device of the hydrogenation Btu utilization that the present invention is provided, the mixture being sequentially connected using pipeline enters
Mouth 1, hydrogenation pre-reactor 2, steam generator 6, hydrogenation tower 11 and hydrogenation oil export 12；The mixture be grease and hydrogen,
The mixing of catalyst, or be aliphatic acid and hydrogen, catalyst mixing.
The hydrogenation pre-reactor first half is provided with highly different multiple outlets, the pipe that these outlets pass through each connection
Steam generator is connected again after road parallel connection；3 outlets arranged from low to high are shown in figure, 3 export the pipe for each communicating with
The first pneumatic on-off valve 3, the second pneumatic on-off valve 4 and the 3rd pneumatic on-off valve 5 are separately installed with road, can be pre- according to hydrogenation
The temperature difference of reactor outlet material is separately turned on.Generally, when the reaction mass temperature in hydrogenation pre-reactor is too high, can carry
Preceding discharging (opening the first pneumatic on-off valve or the second pneumatic on-off valve)；Reaction mass temperature in dihydro pre-reactor is too low
When, discharging (opening the 3rd pneumatic on-off valve or the second pneumatic on-off valve) can be postponed.
The steam output of the soft water input pipe and output steam of input soft water is connected with the steam generator
Pipe；The first pneumatic control valve 7 is provided with the soft water pipeline, the liquid level gauge LT with steam generator realizes chain control, to steaming
The liquid level of vapour generator is controlled；The jet chimney is provided with the second pneumatic control valve 9, with the pressure on steam generator
Sensor PT realizes chain control, and the pressure to steam generator is controlled.Above chain control also can be by DCS system reality
It is existing, or realized by artificial operation.
The hydrogenation pre-reactor can cover (the i.e. one hydrogenation multiple steamings of pre-reactor concatenation of connecting with steam generator more
Vapour generator, also multiple can hydrogenate pre-reactors and concatenate a steam generator).
A kind of recovery method of hydrogenation heat that the present invention is provided, follows the steps below：
1) mixture 1 enters pre-reactor 2, and preliminary hydrogenation is carried out in pre-reactor；According to the height of reaction temperature
It is low, open the first pneumatic on-off valve 3 or the second pneumatic on-off valve 4 or the 3rd pneumatic on-off valve 5 is adjusted；Hydrogenation pre-reactor
Outlet mass temperatures are controlled at 180-230 DEG C；
2) material exported after preliminary hydrogenation enters steam generator, and heat exchange, soft water absorption are carried out with soft water 8
The output of steam 9 produced after heat is incorporated to plant area's steam pipe system, and then realizes the recycling of heat；
3) entered back into hydrogenation tower by the material after steam generator heat exchange and proceed hydrogenation；In hydrogenation tower
Reaction temperature regulation, by the unlatching of the first pneumatic on-off valve 3 or the second pneumatic on-off valve 4 or the 3rd pneumatic on-off valve 5 or
Close and realize.
Described soft water is input into steam generator by soft water pipeline；The first pneumatic control valve set in the soft water pipeline
7 chain with the liquid level gauge LT of steam generator (dotted line represents the data wire being connected in figure；It is as follows), so as to steam generation
The liquid level of device is controlled.Also the liquid level of steam generator can be controlled using manual mode of operation.
Described steam exports steam generator by jet chimney；The jet chimney is provided with the second pneumatic control valve 9
It is chain with pressure sensor PT on steam generator, so as to the steam pressure to steam generator is controlled.Also can use
Manual mode of operation is controlled to the steam pressure of steam generator.
All devices and supporting component in the present invention directly it is outer available from.
Arrow expression thing direction of flow in figure.
Embodiment 1
The mixture of commercial grease (initial iodine number is 96gI/100g), hydrogen and catalyst, enters according to the flow of 15t/h
Enter and carry out hydrogenation in pre-reactor 2；The reaction temperature (hydrogenation pre-reactor outlet mass temperatures) of pre-reactor is increased to
The first pneumatic on-off valve 3 is opened at 230 DEG C, the material after the initial reaction of output carries out heat into steam generator 6 and soft water 8
Amount is exchanged, and control temperature produces 0.6 ton of 0.8Mpa steam per hour to 180 DEG C, is incorporated to plant area's steam pipe system.Sent out by steam
Material after raw device heat exchange proceeds hydrogenation in then entering back into hydrogenation tower；The finished product iodine number of acquisition is less than 5gI/
100g。
Embodiment 2
The mixture 1 of commercial fatty acids (initial iodine number is 74gI/100g), hydrogen and catalyst, enters pre- according to 10t/h
Hydrogenation is carried out in reactor 2；The reaction temperature (hydrogenation pre-reactor outlet mass temperatures) of pre-reactor is increased to 225 DEG C
When open the second pneumatic on-off valve 4, the material after the initial reaction of output carries out heat friendship into steam generator 6 and soft water 8
Change, control temperature produces 0.5 ton of 0.8Mpa steam per hour to 180 DEG C, is incorporated to plant area's steam pipe system.By steam generator
Material after heat exchange proceeds hydrogenation in then entering back into hydrogenation tower；The finished product of acquisition, iodine number is less than 3gI/100g.
Claims (7)
1. a kind of hydrogenation apparatus of recyclable heat of reaction, including the hydrogenation tower (11) for being provided with hydrogenation oil export (12)；Its
It is characterised by that the device accesses the mixture inlet (1) of hydrogenation tower entrance, hydrogenation in advance again after being also sequentially connected using pipeline
Reactor (2) and steam generator (6)；
The hydrogenation pre-reactor first half is provided with highly different multiple outlets, and these outlets are by each communicating with and with gas
Steam generator is connected again after the pipeline parallel connection of dynamic switch valve, is separately turned on the temperature difference according to reaction mass；
The soft water input pipe of input soft water and the steam output pipe of output steam are connected with the steam generator.
2. hydrogenation apparatus of recyclable heat of reaction according to claim 1, it is characterised in that：The soft water pipeline
In be provided with the first pneumatic control valve (7), the pneumatic control valve carries out chain control with the liquid level gauge (LT) of steam generator；It is described
The second pneumatic control valve (9) is provided with jet chimney, the pneumatic control valve enters with the pressure sensor (PT) on steam generator
Row chain control.
3. hydrogenation apparatus of recyclable heat of reaction according to claim 2, it is characterised in that：The mixture is
Grease or aliphatic acid, the mixing with hydrogen and catalyst.
4. hydrogenation apparatus of recyclable heat of reaction according to claim 3, it is characterised in that：The hydrogenation is pre- anti-
Answer device with steam generator to cover series system more.
5. a kind of recovery method of hydrogenation heat, follows the steps below：
1) in mixture input hydrogenation pre-reactor (2), preliminary hydrogenation is carried out in pre-reactor is hydrogenated；The hydrogenation is pre-
Reactor outlet material temperature control is at 180-230 DEG C；
2) material of hydrogenation pre-reactor outlet output enters steam generator (6), and heat exchange is carried out with soft water (8), passes through
After steam generator heat exchange cooling, to enter back into and proceed hydrogenation in hydrogenation tower (11)；Then discharging exports finished product；
3) soft water enters steam generator, absorbs the steam (9) produced after heat and is incorporated to plant area's steam pipe system.
6. the recovery method of hydrogenation heat according to claim 5, it is characterised in that：Step 1) in, hydrogenate pre- anti-
The outlet mass temperatures of device are answered, by adjusting the first pneumatic on-off valve (3), the second pneumatic on-off valve (4) and the 3rd pneumatic opening
The different opening for closing valve (5) is controlled.
7. the recovery method of hydrogenation heat according to claim 6, it is characterised in that：Step 3) in, in hydrogenation tower
Reaction temperature section, by being turned on and off for the first pneumatic on-off valve, the second pneumatic on-off valve and the 3rd pneumatic on-off valve
Realize.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611245885.7A CN106753818A (en) | 2016-12-29 | 2016-12-29 | The hydrogenation apparatus and heat of reaction recovery method of a kind of recyclable heat of reaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611245885.7A CN106753818A (en) | 2016-12-29 | 2016-12-29 | The hydrogenation apparatus and heat of reaction recovery method of a kind of recyclable heat of reaction |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106753818A true CN106753818A (en) | 2017-05-31 |
Family
ID=58928830
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611245885.7A Pending CN106753818A (en) | 2016-12-29 | 2016-12-29 | The hydrogenation apparatus and heat of reaction recovery method of a kind of recyclable heat of reaction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106753818A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4847016A (en) * | 1986-01-29 | 1989-07-11 | Henkel Kommanditgesellschaft Auf Aktien | Process for the continuous hydrogenation of fats, fatty acids and fatty acid derivatives in the presence of a heterogeneous catalyst |
| US20100069690A1 (en) * | 2006-10-06 | 2010-03-18 | Nicholas John Gudde | Hydrogenation process |
| CN203754684U (en) * | 2014-03-24 | 2014-08-06 | 山东润银生物化工股份有限公司 | Stearic acid loop hydrogenation reactor |
-
2016
- 2016-12-29 CN CN201611245885.7A patent/CN106753818A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4847016A (en) * | 1986-01-29 | 1989-07-11 | Henkel Kommanditgesellschaft Auf Aktien | Process for the continuous hydrogenation of fats, fatty acids and fatty acid derivatives in the presence of a heterogeneous catalyst |
| US20100069690A1 (en) * | 2006-10-06 | 2010-03-18 | Nicholas John Gudde | Hydrogenation process |
| CN203754684U (en) * | 2014-03-24 | 2014-08-06 | 山东润银生物化工股份有限公司 | Stearic acid loop hydrogenation reactor |
Non-Patent Citations (2)
| Title |
|---|
| 刘玉兰等: "《现代植物油料油脂加工技术》", 30 June 2015, 河南科学技术出版社 * |
| 区灿棋、吕德伟: "《石油化工氧化反应工程与工艺》", 31 July 1992, 中国石化出版社 * |
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| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: Hangzhou City, Zhejiang province 311305 City Shangcheng District No. 128 Lane Applicant after: ZANYU TECHNOLOGY GROUP CO.,LTD. Applicant after: HANGZHOU OLEOCHEMICALS CO.,LTD. Address before: Qingshan Lake Science and Technology City Xingang Ling'an Road, Hangzhou City, Zhejiang Province, No. 628 311305 Applicant before: ZANYU TECHNOLOGY GROUP CO.,LTD. Applicant before: HANGZHOU OLEOCHEMICALS CO.,LTD. |
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| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170531 |