CN105907481A - Alternating serial reaction device for producing biodiesel from high-pressure gas-phase methanol - Google Patents
Alternating serial reaction device for producing biodiesel from high-pressure gas-phase methanol Download PDFInfo
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- CN105907481A CN105907481A CN201610464443.5A CN201610464443A CN105907481A CN 105907481 A CN105907481 A CN 105907481A CN 201610464443 A CN201610464443 A CN 201610464443A CN 105907481 A CN105907481 A CN 105907481A
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- methanol
- high pressure
- gas
- reactor
- reaction mechanism
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Classifications
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- 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
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
- C11C3/10—Ester interchange
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses an alternating serial reaction device for producing biodiesel from high-pressure gas-phase methanol. The device comprises a first-stage reaction mechanism and a second-stage reaction mechanism. In each reaction mechanism, a discharge opening of a reactor is communicated with an inlet of a circulation pump through a grease outlet pipeline, an outlet of the circulation pump is communicated with a material circulation feeding pipe and the reactor to the position below a methanol uniform distributor, a high-pressure methanol main gas inlet pipeline is communicated with a grease inlet pipeline, and a high-pressure gas-phase methanol auxiliary gas inlet pipeline is led to the methanol uniform distributor on the lower portion of the reactor through a built-in reactor top gas inlet pipe. Methanol outlet pipelines are communicated with the high-pressure methanol auxiliary gas inlet pipelines through the methanol circulation pipelines between the first-stage reaction mechanism and the second-stage reaction mechanism. The fixed parallel-connection and non-fixed serial reaction device is formed and provided with a dual-effect stirring system and is high in production efficiency, redundant methanol of the first-stage reaction mechanism can be fully used for second-stage reaction, methanol consumption of a reaction system is remarkably reduced, methanol circulation volume is reduced, and energy consumption is reduced.
Description
Technical field
The present invention relates to organic chemical industry and produce equipment, specially one is alternately used in series high pressure vapor methanol
Produce the reaction unit of biodiesel.
Background technology
Along with socioeconomic fast development, petroleum-based energy is faced with unprecedented crisis, is finding
During new forms of energy, biodiesel receives significant attention as a kind of novel energy.
The main method producing biodiesel at present is esterification ester-interchange method, will animal and plant fat or discarded
The low-carbon alcohols such as oils and fats and methanol carry out being esterified ester exchange reaction (mainly using acid or alkali as catalyst), raw
Become fatty acid methyl ester, i.e. biodiesel.
Esterification process the most accomplished continuously or intermittently two kinds of reaction formations, and intermittent reaction formal cause equipment investment
Little, production process is easily controllable, its service condition is the most universal.Intermittent reaction mainly uses still reaction
Device carries out independent operation, and each still all uses the alcohol oil rate of excess to react, and methanol steam more than needed is the most straight
Tap into into methanol rectification retracting device；On the one hand, each reactor independently carries out esterification, anti-in esterification
Though methanol purity of should having more than needed in the later stage is higher, but methanol more than needed utilizes without secondary, course of reaction use ratio of methanol
Low, both add the load of methanol recovery device, also exacerbate the volatilization loss of Methanol Recovery process；Separately
On the one hand, recycling after the purified condensation of methanol steam more than needed, methanol is experiencing repeatedly phase transition process
In, cause methanol loop amount big, reaction heating system energy consumption is high, increases production cost.
Summary of the invention:
For the deficiencies in the prior art, the technical problem to be solved is to propose a kind of raising ester
Change reaction rate, improve use ratio of methanol, improve production efficiency be alternately used in series high pressure vapor methanol
Produce the reaction unit of biodiesel.
Can solve the problem that above-mentioned technical problem is alternately used in series the anti-of high pressure vapor methanol production biodiesel
Answering device, its technical scheme includes that I and II reaction mechanism, each reaction mechanism include reactor, circulation
Pump and gas-phase methanol are provided with methanol gas uniform device, reactor into and out of pipeline, the bottom of described reactor
The import by grease outlets pipeline communication circulating pump of the discharging opening of bottom, described circulation delivery side of pump passes through
Matter Transfer feed pipe is passed through reactor to below methanol gas uniform device, and described gas-phase methanol is into and out of pipe
Road includes the major and minor admission line of high pressure vapor methanol and methanol gas outlet pipe, described high pressure vapor
Methanol main admission line connection Matter Transfer feed pipe, described high pressure vapor methanol pair admission line is by interior
The still jacking trachea put causes the methanol gas uniform device of reactor bottom；The methanol gas of first order reaction mechanism
By methanol gas string between the high pressure vapor methanol pair admission line of body outlet pipe and secondary response mechanism
Connection pipeline communication, the methanol gas outlet pipe of secondary response mechanism and the high pressure vapor of first order reaction mechanism
Connected by another methanol gas serial pipe between methanol pair admission line；Described each pipeline is provided with
Control valve.
For making methanol gas and reaction oils and fats uniformly and be fully contacted, the one of described methanol gas uniform device
Structure uses surface uniformly to offer the endless tube of venthole, and described endless tube is co-axially mounted with reactor.
In conventional design, the main admission line of high pressure vapor methanol of I and II reaction mechanism and high pressure vapor
Methanol pair admission line parallel communication high-pressure methanol steam generator.
In conventional design, the methanol gas outlet pipe parallel communication methanol gas of I and II reaction mechanism
Recovery tower.
Beneficial effects of the present invention:
1, the present invention is alternately used in series the reaction unit of high pressure vapor methanol production biodiesel by arranging
In reactor outer loop pump circulation stirring reaction mass and reactor, methanol gas distributor increases methanol gas
Body contacts with the stirring mixing of reaction mass, forms economic benefits and social benefits stirring system, is conducive to improving gas-liquid mass transfer effect
Rate, makes reaction mass and methanol gas be sufficiently mixed, uniform contact, makes reaction more abundant, and can and
Time get rid of byproduct of reaction (water), make reaction to generate biodiesel direction carry out, make esterification more
Thoroughly, thus improve esterification reaction rate.
2, the present invention is by the way of fixed parallel connection and free-standing series combination, and high-purity is used alternatingly
Gas-phase methanol, and by series connection secondary response mechanism pair admission line by the methanol more than needed of first order reaction mechanism
React for secondary facility, decrease the latent heat of phase change of methanol recycling, greatly reduce gas-phase methanol
Usage amount, reduces refined recovery quantity of methyl alcohol, and use ratio of methanol significantly improves, and has saved energy consumption.
3, the present invention is during circulation oils and fats and high pressure vapor methanol mixed, respectively at oils and fats circulation pipe and
Form tubular type high pressure and autoclave low pressure coupled reaction system in reactor, be conducive to accelerating reaction rate, and
The degree of depth breaks chemical equilibrium, improves oils and fats overall conversion, improves production efficiency.
Accompanying drawing explanation
Fig. 1 be one embodiment of the present invention operation principle schematic diagram.
Figure number identifies: 1, reactor；2, circulating pump；3, discharging opening；4, grease outlets pipeline；5、
Matter Transfer feed pipe；6, the main admission line of high pressure vapor methanol；7, high-pressure methanol gas pair air inlet pipe
Road；8, methanol gas outlet pipe；9, methanol gas uniform device；10, methanol gas serial pipe；
11, valve is controlled.
Detailed description of the invention
Hereinafter the preferred embodiment of technical solution of the present invention is further described, it should be appreciated that this
Preferred embodiment described by place is merely to illustrate and explains that the present invention makes it easy to understand, is not used to limit
Determine the present invention.
The present invention is used alternatingly high-pressure methanol and produces the reaction unit of biodiesel, and the one-level including left side is anti-
Answering the secondary response mechanism on mechanism and right side, the configuration of each reaction mechanism is identical, all include reactor 1,
Circulating pump 2 and methanol gas are into and out of pipeline, as shown in Figure 1.
In each reaction mechanism, the bottom in reactor 1 is provided with methanol gas uniform device 9, described methanol gas
Body uniform device 9 is endless tube coaxial mounted with reactor 1, uniform on described endless tube offers venthole；
Described circulating pump 2 is located at outside reactor 1, and the import of circulating pump 2 is connected instead by grease outlets pipeline 4
Answering the discharging opening 3 bottom still 1, the outlet of circulating pump 2 connects reactor 1 by Matter Transfer feed pipe 5
Discharging opening 3, and opened inwards into reactor 1 by discharging opening 3, it is equal that position is in methanol gas
The central lower of cloth device 9, described each pipeline is provided with control valve 11, as shown in Figure 1.
Described methanol gas includes the main admission line of high pressure vapor methanol 6, high-pressure methanol gas into and out of pipeline
Body pair admission line 7 and methanol gas outlet pipe 8, described high pressure vapor methanol main admission line 6 is even
Lead on the Matter Transfer feed pipe 5 in circulating pump 2 exit, described high-pressure methanol gas pair admission line
7 are caused (connection) methanol gas uniform device 9, described methanol gas escape pipe by built-in still jacking trachea
Road 8 is from gas outlet, the top pass-out of reactor 1, and described each pipeline is provided with control valve 11, such as Fig. 1
Shown in.
One-level, secondary response mechanism methanol gas outlet pipe 8 parallel communication to methanol gas recovery tower,
Recycle after refined for band water methanol gas, one-level, the main air inlet of high pressure vapor methanol of secondary response mechanism
Pipeline 6 and high-pressure methanol gas pair admission line 7 parallel communication are to high pressure methanol steam generator；One-level
The methanol gas outlet pipe 8 of reaction mechanism and the high-pressure methanol gas pair admission line of secondary response mechanism
Connected by methanol gas serial pipe 10 between 7, the methanol gas outlet pipe 8 of secondary response mechanism
And connected by another methanol gas between the high-pressure methanol gas pair admission line 7 of first order reaction mechanism
Pipeline 10 connects, and described each pipeline is provided with control valve 11, as shown in Figure 1.
The method of operation of the present invention:
1, after first order reaction still 1 and secondary response still 1 feed, add acid catalyst simultaneously, start circulation
Pump 2 recycle stock, opens the first order reaction still 1 methanol gas serial pipe 10 to secondary response still 1,
Open the methanol gas outlet pipe 8 of secondary response still 1, open the high pressure vapor first of first order reaction still 1
Opening of the main admission line of alcohol 6, suitably the high-pressure methanol gas pair admission line 7 of regulation secondary response still 1
Qi Du, forms cascade reaction system.
2, after first order reaction still 1 lactonization reaction terminates, the high pressure vapor methanol of first order reaction still 1 is closed
Main admission line 6, closes the first order reaction still 1 methanol gas serial pipe 10 to secondary response still 1,
Open the methanol gas outlet pipe 8 of first order reaction still 1, close the high-pressure methanol gas of secondary response still 1
Body pair admission line 7, opens the main admission line of high pressure vapor methanol 6 of secondary response still 1, discharges one-level
The esterifying liquid of reactor 1.
3, first order reaction still 1 feeds again, added acid-catalyst, opens secondary response still 1 to first order reaction
The methanol gas serial pipe 10 of still 1, closes the methanol gas outlet pipe 8 of secondary response still 1；Extremely
This, complete first order reaction still 1 and secondary response still 1 alternately, the most original secondary response still 1 changes
For first order reaction still, first order reaction still 1 originally is changed into secondary response still 1, because original two grades anti-
Answer still 1 to utilize first order reaction still methanol of having more than needed to carry out pre-esterification, therefore, change at secondary response still 1
For first order reaction still and when using fresh high pressure vapor methanol to react, its methanol purity more than needed discharged is higher,
It is sufficient for the first order reaction still primary esterification demand to methanol purity.Can by operating above mode
To find out:
1, it is the methanol more than needed making full use of reaction mechanism, and breaks Equilibrium limit, improve reaction speed
Rate, first order reaction still 1 is passed through fresh high pressure vapor methanol, and methanol more than needed is by methanol gas tandem tube
Road 10 enters secondary response still 1 and reacts.
2, for improving production efficiency, first order reaction still 1 and secondary response still 1 use free-standing to connect,
Due to the esterification initial stage, the moisture that reaction system produces is more, by the control valve door operation of pipeline,
First order reaction still 1 can be made to use fresh high pressure vapor methanol steam to carry out deep reaction oils and fats, and obtain follows
Ring methanol gas is aqueous few, and purity is high, and circulation gas-phase methanol enters the methanol gas of secondary response still 1 and divides
Cloth device, the circulation stirring reaction oils and fats outside association reaction mechanism, make methanol and oil in secondary response still 1
Fat is abundant, uniform contact, and esterification is quickly carried out.
3, it is passed through form by control reaction mechanism methanol gas, is alternately used in series high pressure vapor methanol,
Avoid that to there is methanol gas utilization rate in independent in parallel reaction mechanism low, the defect that energy consumption is excessive.
Claims (4)
- The most alternately being used in series the reaction unit of high pressure vapor methanol production biodiesel, its feature exists In: include that I and II reaction mechanism, each reaction mechanism include reactor (1), circulating pump (2) It is provided with methanol gas uniform device (9) into and out of pipeline, the bottom of described reactor (1) with gas-phase methanol, The discharging opening (3) of reactor (1) bottom is by grease outlets pipeline (4) communication loop pump (2) Import, the outlet of described circulating pump (2) is passed through reactor (1) by Matter Transfer feed pipe (5) To methanol gas uniform device (9) lower section, described gas-phase methanol includes high pressure vapor first into and out of pipeline The main admission line of alcohol (6) and high pressure vapor methanol pair admission line (7) and methanol gas escape pipe Road (8), the main admission line of described high pressure vapor methanol (6) connection Matter Transfer feed pipe (5), It is equal that described gas-phase high pressure methanol pair admission line (7) is caused methanol gas by built-in still jacking trachea Cloth device (9)；The methanol gas outlet pipe (8) of first order reaction mechanism and the height of secondary response mechanism Connected by methanol gas serial pipe (10) between pressure methanol gas pair admission line (7), two The methanol gas outlet pipe (8) of order reaction mechanism is secondary with the high pressure vapor methanol of first order reaction mechanism Connected by another methanol gas serial pipe (10) between admission line (7)；Described each pipe Road is provided with control valve (11).
- The most according to claim 1 alternately it is used in series high pressure vapor methanol production biodiesel Reaction unit, it is characterised in that: described methanol gas uniform device (9) is that surface uniformly offers The endless tube of venthole, described endless tube is co-axially mounted with reactor (1).
- 3. according to claim 1 or described be alternately used in series high pressure vapor methanol production biology bavin The reaction unit of oil, it is characterised in that: the main air inlet pipe of high pressure vapor methanol of I and II reaction mechanism Road (6) and high pressure vapor methanol pair admission line (7) parallel communication high-pressure methanol steam generator.
- 4. according to claim 1 or described be alternately used in series high pressure vapor methanol production biology bavin The reaction unit of oil, it is characterised in that: the methanol gas outlet pipe (8) of I and II reaction mechanism Parallel communication methanol gas recovery tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610464443.5A CN105907481B (en) | 2016-06-23 | 2016-06-23 | Alternating is used in series the reaction unit of high pressure vapor methanol production biodiesel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610464443.5A CN105907481B (en) | 2016-06-23 | 2016-06-23 | Alternating is used in series the reaction unit of high pressure vapor methanol production biodiesel |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105907481A true CN105907481A (en) | 2016-08-31 |
| CN105907481B CN105907481B (en) | 2019-05-31 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610464443.5A Expired - Fee Related CN105907481B (en) | 2016-06-23 | 2016-06-23 | Alternating is used in series the reaction unit of high pressure vapor methanol production biodiesel |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107670629A (en) * | 2017-11-09 | 2018-02-09 | 大丰鑫源达化工有限公司 | A kind of device that salt is analysed using tail gas acid gas |
| CN109320542A (en) * | 2018-11-13 | 2019-02-12 | 江西宏柏新材料股份有限公司 | Double kettles series connection synthetic method of the silane coupling agent of the propyl containing mercapto |
| US11814349B1 (en) | 2022-08-03 | 2023-11-14 | Inventure Renewables, Inc. | Processes for organic acid alkyl ester production using low pressure alkylation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201704307U (en) * | 2010-04-21 | 2011-01-12 | 潍坊市大明化工有限公司 | Esterification reaction device for fatty acid methyl ester |
| CN104152275A (en) * | 2014-08-22 | 2014-11-19 | 防城港市中能生物能源投资有限公司 | Gas-phase methanol esterification reaction device |
| CN204455054U (en) * | 2015-03-10 | 2015-07-08 | 乐山纯一新能源科技有限公司 | A kind of esterification system for production of biodiesel |
-
2016
- 2016-06-23 CN CN201610464443.5A patent/CN105907481B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201704307U (en) * | 2010-04-21 | 2011-01-12 | 潍坊市大明化工有限公司 | Esterification reaction device for fatty acid methyl ester |
| CN104152275A (en) * | 2014-08-22 | 2014-11-19 | 防城港市中能生物能源投资有限公司 | Gas-phase methanol esterification reaction device |
| CN204455054U (en) * | 2015-03-10 | 2015-07-08 | 乐山纯一新能源科技有限公司 | A kind of esterification system for production of biodiesel |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107670629A (en) * | 2017-11-09 | 2018-02-09 | 大丰鑫源达化工有限公司 | A kind of device that salt is analysed using tail gas acid gas |
| CN107670629B (en) * | 2017-11-09 | 2023-08-22 | 大丰鑫源达化工有限公司 | Device for separating salt from acid gas by utilizing tail gas |
| CN109320542A (en) * | 2018-11-13 | 2019-02-12 | 江西宏柏新材料股份有限公司 | Double kettles series connection synthetic method of the silane coupling agent of the propyl containing mercapto |
| US11814349B1 (en) | 2022-08-03 | 2023-11-14 | Inventure Renewables, Inc. | Processes for organic acid alkyl ester production using low pressure alkylation |
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| CN105907481B (en) | 2019-05-31 |
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Effective date of registration: 20190612 Address after: 538000 No. 7 Kangchen Third Lane, Xiwan Square, Fangchenggang Port District, Guangxi Zhuang Autonomous Region (C36, former Kangchen District) Patentee after: Fangchenggang Sanhua Energy Co.,Ltd. Address before: 538001 Building C35 and C36 of Kangchen District, Fangchenggang Port District, Guangxi Zhuang Autonomous Region Patentee before: FANGCHENGGANG ZHONGNENG BIOENERGY INVESTMENT CO.,LTD. |
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Effective date of registration: 20200106 Address after: Room 1904, 19 / F, Hing Fu centre, 11-12 Dexing street, Kowloon, Hong Kong, China Patentee after: Zhongze International Co.,Ltd. Address before: 538000 No. 7 Kangchen Third Lane, Xiwan Square, Fangchenggang Port District, Guangxi Zhuang Autonomous Region (C36, former Kangchen District) Patentee before: Fangchenggang Sanhua Energy Co.,Ltd. |
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Granted publication date: 20190531 |