CN100412170C - Process for preparing biological diesel oil by using loop reactor - Google Patents
Process for preparing biological diesel oil by using loop reactor Download PDFInfo
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- CN100412170C CN100412170C CNB2006101299196A CN200610129919A CN100412170C CN 100412170 C CN100412170 C CN 100412170C CN B2006101299196 A CNB2006101299196 A CN B2006101299196A CN 200610129919 A CN200610129919 A CN 200610129919A CN 100412170 C CN100412170 C CN 100412170C
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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
- 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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- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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Abstract
The invention discloses a manufacturing method of biological diesel in the circulating reactor, which comprises the following steps: adopting circulating reactor and auxiliary equipment with reflux condenser, high-level groove, static blender and pump; dissolving solid alkaline catalyst or solid acid catalyst in the carbinol; adding catalyst into circulating reactor from the top; blending carbinol and grease in the static blender into circulating reactor through pump and cavitation injector; proceeding ester exchange reaction at 50-70 deg.c or 100-160 deg.c under 0.3-1.5Mpa; circulating carbinol from the top of circulating reactor; obtaining glycerin and biological diesel from the bottom of circulating reactor.
Description
Technical field
The present invention relates to a kind ofly, belong to the production of biodiesel technical field with loop reactor production method of bio-diesel oil.
Background technology
Along with the rapid increase of energy demand and the resource limit of the fossil base energy, countries in the world are all in the exploitation of accelerating novel renewable energy.Biofuel is extensively paid close attention to owing to have flammable good, nontoxic, biodegradable, advantage such as cetane value is high, recyclability good, sulfide and CO (carbon monoxide converter) emission are few, has been classified as the new forms of energy product of policy support by countries such as America and Europes.China also classifies the exploitation of biofuel as national medium-term and long-term development program.
Biofuel, be fatty acid methyl ester (or ethyl ester), its production technique is to adopt in alcohols materials such as methyl alcohol or ethanol and crude vegetal or the animal tallow main component tri-glyceride under sour, basic catalyst effect transesterification reaction to take place, utilize methoxyl group to replace glyceryl on the longer chain fatty acid, the fatty acid methyl ester of generation or ethyl ester and by-product glycerin phase-splitting are after wash, obtain after the vacuum hydro-extraction.Transesterification reaction is the key of whole process of production, and its level of response is determining the transformation efficiency and the yield of fatty acid methyl ester or ethyl ester.At present, in the required catalyzer of transesterification reaction, solid alkali or solid acid catalyst are because the catalytic efficiency height, reusable, product separates simple, does not produce or seldom produce salkali waste (acid) liquid, meet Sustainable development green chemical industry industry direction, and be widely adopted.Based on above-mentioned ester exchange process production biofuel, currently used reactor is a stirred-tank reactor.Yet, because the transesterification reaction under solid alkali (acid) catalysis is a typical air-liquid-solid three-phase heterogeneous reaction system, carrying out transesterification reaction in stirred-tank reactor, to have an alternate mixing inhomogeneous, resistance to mass transfer increases, there is shortcomings such as " dead bands " in the reactor, often cause the transesterify time lengthening, product production and yield reduce, and directly have influence on the production cost and the quality product of biofuel; Simultaneously, the power consumption of keeping reaction is bigger, and the solid catalyst wearing and tearing are more obvious.Therefore, the transesterification reactor of development of new and reaction process, further improve and promote alternate mixing in the reactor, reduce the interphase mass transfer resistance, shorten the reaction times,, prevent the loss of solid base catalyst for improving product yield, reduce production costs, simplify production technique and have great importance for the biofuel suitability for industrialized production.
Summary of the invention
The object of the invention is to provide that a kind of it is simple that this method has production process with loop reactor production method of bio-diesel oil, and energy consumption is low, the characteristics that the biofuel transformation efficiency is high.
The present invention is realized by following technical proposals: a kind of with loop reactor production method of bio-diesel oil, this method adopts and comprises the loop reactor main equipment, and utility appliance reflux exchanger, header tank, static mixer and pump, described loop reactor is by cylindrical housings, the intravital guide shell of shell, with the guide shell concentric position cavitating nozzle is set on the bottom of housing, the top of housing is provided with the air-liquid-solid triphase separator; The aspect ratio of its middle shell is 3: 1～7: 1, and the aspect ratio of guide shell is 2: 1～5: 1; With methyl alcohol and comprise that the grease of animal-plant oil, waste edible oil and sewer oil is a raw material, be that catalyzer carries out transesterification reaction production biofuel with the solid alkali, it is characterized in that comprising following process:
1. the solid base catalyst Mg-Al that will form for the presoma roasting with the hydrotalcite, or be the solid base catalyst MgO/CaO of carrier loaded magnesium oxide (MgO) with calcium oxide (CaO), or with the solid base catalyst KF/MgO of magnesium oxide carrying potassium oxide (KF), or with the solid base catalyst KF/CaO of calcium oxide carrying potassium oxide (KF), be dissolved in the opening for feed adding loop reactor of methyl alcohol by the loop reactor top, catalyst consumption is 0.2%～1% of an oil quality.
2, be 6～60: 1 in molar ratio with methyl alcohol and grease, methyl alcohol and grease is mixed through static mixer, enter loop reactor with the linear speed of 5～40m/s through the loop reactor bottom through pump and cavitating nozzle again, methyl alcohol and grease feed liquid 50～70 ℃ of temperature, are carried out transesterification reaction 30～90min in loop reactor.
3, the methanol steam header tank of flowing through after the reflux exchanger condensation is gone into static mixing tank with the mixing of materials of loop reactor top discharge mouth extraction is laggard then, enters loop reactor through pump, nozzle and realizes the methanol loop utilization.
4, byproduct glycerine is discharged and is collected from loop reactor bottom discharge mouth, and the major product biofuel is discharged and collected from loop reactor top discharge mouth and loop reactor bottom discharge mouth respectively.
With above-mentioned loop reactor device, with methyl alcohol and comprise that the grease of animal-plant oil, waste edible oil and sewer oil is a raw material, be that catalyzer carries out transesterification reaction production biofuel with the solid acid, it is characterized in that comprising following process:
1. solid heteropoly acid catalyst S O
4 2-/ ZrO
2. or solid acid catalyst iron(ic) chloride (FeCl
3), the opening for feed that is dissolved in loop reactor top behind the methyl alcohol adds loop reactor, and catalyst consumption is 2%～10% of an oil quality.
2, be 6～60: 1 in molar ratio with methyl alcohol and grease, methyl alcohol and grease after static mixer mixes, are entered loop reactor with the linear speed of 5～40m/s through the loop reactor bottom through pump and cavitating nozzle again.In temperature is 100～160 ℃, and pressure is 0.3～1.5MPa, carries out transesterification reaction 60～180min.
3, the methanol steam header tank of flowing through after the reflux exchanger condensation is gone into static mixing tank with the mixing of materials of loop reactor top discharge mouth extraction is laggard then, enters loop reactor through pump, nozzle and realizes the methanol loop utilization.
4, byproduct glycerine is discharged and is collected from loop reactor bottom discharge mouth, and the major product biofuel is discharged and collected from loop reactor top discharge mouth and loop reactor bottom discharge mouth respectively.
The invention has the advantages that: inner guide shell and the air-liquid-solid triphase separator that is provided with of loop reactor effectively increased the partial aspect ratio of loop reactor, eliminated " dead band " in the loop reactor, improved mass transfer and reaction efficiency; The outer circulation pipeline two ends of loop reactor outer setting link to each other with cavitating nozzle with intercepting basin respectively, form the outer circulation loop, the injection by cavitating nozzle makes methyl alcohol and the rapid emulsification of grease, increases the two-phase contact area, strengthen the transesterify process, shortened the reaction times; In addition, this device structure is simple, and cost is low, and methyl alcohol can be recycled, and has increased the alcohol oil rate of reaction process, has strengthened operation of equipment elasticity.Thereby power consumption is big when having overcome traditional stirred-tank reactor production biofuel, gordian technique defective such as the transesterification reaction time is long, and product production and yield are lower.Compare with the stirred-tank reactor production technique, under same reaction conditions, reach identical transformation efficiency, adopt the loop reactor reaction times to shorten more than 10%.This production method is applicable to multiple glyceride stock such as vegetable and animals oils, waste edible oil and trench wet goods are converted into biofuel.The present invention can obtain high yield and high-quality biofuel by utilizing fluidized-bed loop reactor production biofuel.Adopt solid base catalyst, Fatty acid methyl ester purity is 97.1～98.1%, transformation efficiency is 99.3～99.7%, yield is 99.1～99.8% (transformation efficiency=reaction after product amount of substance/product amount of substance * 100% when transforming fully, the quality of the quality/raw material of yield=products therefrom * 100%); Adopt solid acid catalyst, Fatty acid methyl ester purity is 95.5～96.4%, and transformation efficiency is 99.0～99.5%, yield is 95.1～97.3% (for acidifying oil, Fatty acid methyl ester purity is 90.1～92.2%, and transformation efficiency is 91.0～92.5%, and yield is 90.0～92.7%).
Description of drawings
The fluidized-bed loop reactor structural representation of Fig. 1 for realizing that the inventive method adopted.Among the figure, 1 is opening for feed, and 2 is the air-liquid-solid triphase separator, 3 is the cylinder shape housing, and 4 is guide shell, and 5 is cavitating nozzle, 6 is the bottom discharge mouth, 7 is pump, and 8 is controlled asbestos electrically heated cover, and 9 is static mixer, 10 are the top discharge mouth, 11 is intercepting basin, and 12 is header tank, and 13 is reflux exchanger.
Embodiment
The invention will be further described below in conjunction with specific embodiment.
With loop reactor height overall 1m, air-liquid-solid triphase separator diameter of the housing 0.4m, cylindrical housings diameter 0.2m, draft tube diameter 0.15m, it is as follows that the high 0.5m of guide shell, loop reactor effectively adorn the specific embodiment of loop reactor production biofuel of the long-pending 30L of liquid:
The edible rape seed oil of 8kg methyl alcohol and 15kg is mixed, and enter above-mentioned loop reactor with the linear speed of 20m/s, join in the loop reactor with solid base catalyst KF/CaO150g and 0.5kg methanol mixed and through opening for feed through pump and cavitating nozzle.Slow heating ring flow reactor, keep 60 ℃ of the interior temperature of loop reactor, methyl alcohol in the header tank (via static mixer) is pumped into loop reactor, until there being liquid from intercepting basin, to be spilled in the static mixer, suitably regulate the valve switch of header tank bottom, make the liquid level in the header tank keep constant substantially.The mixed solution of the methyl alcohol of loop reactor and rape seed oil is under the injection pushing effect of cavitating nozzle at this moment, in guide shell, acutely mix and move upward, and in whole loop reactor, form circulation, solid catalyst, methyl alcohol and rape seed oil in loop reactor by thorough mixing and transesterification reaction takes place.The methyl alcohol vaporization that a part has neither part nor lot in reaction forms bubble, makes to form the air-liquid-solid three-phase system in the loop reactor, and overflows from liquid level at air-liquid-solid triphase separator place.The methanol steam of effusion liquid level enters the liquefaction that is cooled in the reflux exchanger, and returns in the header tank.In the loop reactor a part of mixed solution via the overflow of air-liquid-solid triphase separator to intercepting basin, and in static mixer, mix mutually with recycle methanol, after the pump supercharging, under the Hydrodynamic cavitation effect of cavitating nozzle, the rapid emulsification of methyl alcohol and rape seed oil, the two-phase contact area is further increased, promote methyl alcohol and rape seed oil that transesterification reaction takes place rapidly in loop reactor, shortened the transesterification reaction time effectively.
Keep above-mentioned reaction conditions 60min, the valve of closing the header tank bottom steams the methyl alcohol in the loop reactor only, is cooled to room temperature and carries out the phase-splitting processing.Earlier byproduct glycerine is discharged and collected from loop reactor bottom discharge mouth, then the major product biofuel is discharged and collected from loop reactor top discharge mouth and loop reactor bottom discharge mouth respectively.It is 97.1% that chromatogram detects Fatty acid methyl ester content, and the Fatty acid methyl ester transformation efficiency is 99.4%, and yield reaches 99.2%; Glycerol content is 92.1%, and yield is 97.2%.
Embodiment 2
8kg methyl alcohol and 13kg edible soybean oil are mixed, and entering above-mentioned loop reactor with the linear speed of 20m/s through pump and cavitating nozzle, solid base catalyst Mg-Al composite oxides 90g that hydrotalcite is formed for the presoma roasting and 0.5kg methanol mixed also add in the loop reactor through opening for feed.And the experimental procedure among the repetition embodiment 1, be cooled to room temperature then and carry out the phase-splitting processing.It is 97.6% that chromatogram detects formicester content, and the Fatty acid methyl ester transformation efficiency is 99.4%, and yield reaches 99.5%; Glycerol content is 91.3%, and yield is 96.2%.
8kg methyl alcohol and 16kg are mixed through pretreated Oleum Gossypii semen, and enter above-mentioned loop reactor with the linear speed of 20m/s, join in the loop reactor with solid base catalyst MgO/CaO160g and 0.5kg methanol mixed and through opening for feed through pump and cavitating nozzle.And the experimental procedure among the repetition embodiment 1, be cooled to room temperature then and carry out the phase-splitting processing.It is 97.4% that chromatogram detects formicester content, and the Fatty acid methyl ester transformation efficiency is 99.5%, and yield reaches 96.5%; Glycerol content is 93.5%, and yield is 94.5%.
With loop reactor height overall 0.7m, air-liquid-solid triphase separator diameter of the housing 0.3m, cylinder shape housing diameter 0.15m, draft tube diameter 0.1m, it is as follows that the high 0.35m of guide shell, loop reactor effectively adorn the specific embodiment of loop reactor production biofuel of the long-pending 10L of liquid:
2.7kg methyl alcohol and 4.3kg are mixed through the waste edible oil of purifying treatment, and enter above-mentioned loop reactor with the linear speed of 15m/s through pump and cavitating nozzle, join in the loop reactor with solid base catalyst KF/MgO150g and 0.5kg methanol mixed and through opening for feed.Slow heating ring flow reactor, keep 65 ℃ of the interior temperature of loop reactor, methyl alcohol in the header tank (via static mixer) is pumped into loop reactor, until there being liquid from intercepting basin, to be spilled in the static mixer, suitably regulate the valve switch of header tank bottom, make the liquid level in the header tank keep constant substantially.The mixed solution of the methyl alcohol of loop reactor and waste edible oil is under the injection pushing effect of cavitating nozzle at this moment, in guide shell, acutely mix and move upward, and in whole loop reactor, form circulation, solid catalyst, methyl alcohol and waste edible oil in loop reactor by thorough mixing and transesterification reaction takes place.The methyl alcohol vaporization that a part has neither part nor lot in reaction forms bubble, makes to form the air-liquid-solid three-phase system in the loop reactor, and overflows from liquid level at air-liquid-solid triphase separator place.The methanol steam of effusion liquid level enters the liquefaction that is cooled in the reflux exchanger, and returns in the header tank.In the loop reactor a part of mixed solution via the overflow of air-liquid-solid triphase separator to intercepting basin, and in static mixer, mix mutually with recycle methanol, after the pump supercharging, under the Hydrodynamic cavitation effect of cavitating nozzle, the rapid emulsification of methyl alcohol and waste edible oil, the two-phase contact area is further increased, promote methyl alcohol and waste edible oil that transesterification reaction takes place rapidly in loop reactor, shortened the transesterification reaction time effectively.
Keep above-mentioned reaction conditions 150min, the valve of closing the header tank bottom steams the methyl alcohol in the loop reactor only, is cooled to room temperature and carries out the phase-splitting processing.Earlier byproduct glycerine is discharged and collected from loop reactor bottom discharge mouth, then the major product biofuel is discharged and collected from loop reactor top discharge mouth and loop reactor bottom discharge mouth respectively.It is 95.6% that chromatogram detects formicester content, and the Fatty acid methyl ester transformation efficiency is 99.0%, and yield reaches 98.5%; Glycerol content is 90.6%, and yield is 94.2%.
2.7kg methyl alcohol and 4.3kg are mixed through pretreated acidifying oil (acid number 46mgKOH/g), and enter above-mentioned loop reactor with the linear speed of 15m/s, with solid acid catalyst SO through pump and cavitating nozzle
4 2-/ ZrO
2160g and 0.5kg methanol mixed also add loop reactor through opening for feed.And the experimental procedure among the repetition embodiment 4, be cooled to room temperature then and carry out the phase-splitting processing.It is 90.4% that chromatogram detects formicester content, and the Fatty acid methyl ester transformation efficiency is 91.2%, and yield reaches 92.5%; Glycerol content is 88.6%, and yield is 91.5%.
2.7kg methyl alcohol and 4.3kg are mixed through pretreated frying waste oil, and enter above-mentioned loop reactor with the linear speed of 15m/s, with solid acid catalyst FeCl through pump and cavitating nozzle
3160g and 0.5kg methanol mixed and in opening for feed adds loop reactor.And the experimental procedure among the repetition embodiment 4, be cooled to room temperature then and carry out the phase-splitting processing.It is 96.7% that chromatogram detects formicester content, and the Fatty acid methyl ester transformation efficiency is 95.1%, and yield reaches 94.5%; Glycerol content is 92.3%, and yield is 94.7%.
Claims (2)
1. one kind with loop reactor production method of bio-diesel oil, this method adopts and comprises the loop reactor main equipment, and utility appliance reflux exchanger, header tank, the device that static mixer and pump constitute, described loop reactor main equipment is by cylindrical housings, the intravital guide shell of shell, on the bottom of housing with the cavitating nozzle of the concentric setting of guide shell, the air-liquid-solid triphase separator that housing top is provided with constitutes, wherein the aspect ratio of cylindrical housings is 3: 1～7: 1, the aspect ratio of guide shell is 2: 1～5: 1, and with methyl alcohol with comprise animal-plant oil, the grease of waste edible oil and sewer oil is a raw material, with the solid alkali is that catalyzer carries out transesterification reaction production biofuel, it is characterized in that comprising following process:
1). the solid base catalyst Mg-Al that will form for the presoma roasting with the hydrotalcite, or be carrier loaded magnesian solid base catalyst MgO/CaO with calcium oxide, or with the solid base catalyst KF/MgO of magnesium oxide carrying potassium oxide, or with the solid base catalyst KF/CaO of calcium oxide carrying potassium oxide, be dissolved in methyl alcohol, opening for feed by the loop reactor top adds loop reactor, and catalyst consumption is 0.2%～1% of an oil quality;
2). is 6～60 in molar ratio with methyl alcohol with grease: 1 after static mixer mixes, enter loop reactor with the linear speed of 5～40m/s through the loop reactor bottom through pump and cavitating nozzle again, in temperature is under 50～70 ℃ of conditions, carries out transesterification reaction 30～90min;
3). the methanol steam header tank of after the reflux exchanger condensation, flowing through, go into static mixing tank with the mixing of materials of loop reactor top discharge mouth extraction is laggard then, enter loop reactor through pump, nozzle and realize the methanol loop utilization;
4). byproduct glycerine is discharged and is collected from loop reactor bottom discharge mouth, and the major product biofuel is discharged and collected from loop reactor top discharge mouth and loop reactor bottom discharge mouth respectively.
2. one kind with loop reactor production method of bio-diesel oil, this method adopts and comprises the loop reactor main equipment, and the device of utility appliance reflux exchanger, header tank, static mixer and pump formation, described loop reactor main equipment is by cylindrical housings, the intravital guide shell of shell, on the bottom of housing with the cavitating nozzle of the concentric setting of guide shell, the air-liquid-solid triphase separator that housing top is provided with constitutes, the aspect ratio of its middle shell is 3: 1～7: 1, and the aspect ratio of guide shell is 2: 1～5: 1; And with methyl alcohol and comprise that the grease of animal-plant oil, waste edible oil and sewer oil is a raw material, be that catalyzer carries out transesterification reaction production biofuel with the solid acid, it is characterized in that comprising following process:
1). solid heteropoly acid catalyst S O
4 2-/ ZrO
2, or solid acid catalyst iron(ic) chloride, be dissolved in methyl alcohol, by the opening for feed adding loop reactor at loop reactor top, catalyst consumption is 2%～10% of an oil quality;
2). is 6～60 in molar ratio with methyl alcohol with grease: 1 after static mixer mixes, enter loop reactor with the linear speed of 5～40m/s through the loop reactor bottom through pump and cavitating nozzle again, being 100～160 ℃ in temperature is under 0.3～1.5MPa condition with pressure, carries out transesterification reaction 60～180min;
3). the methanol steam header tank of after the reflux exchanger condensation, flowing through, go into static mixing tank with the mixing of materials of loop reactor top discharge mouth extraction is laggard then, enter loop reactor through pump, nozzle and realize the methanol loop utilization;
4). byproduct glycerine is discharged and is collected from loop reactor bottom discharge mouth, and the major product biofuel is discharged and collected from loop reactor top discharge mouth and loop reactor bottom discharge mouth respectively.
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| CNB2006101299196A CN100412170C (en) | 2006-12-07 | 2006-12-07 | Process for preparing biological diesel oil by using loop reactor |
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| CN101469273B (en) * | 2007-12-25 | 2013-03-13 | 亚炬企业股份有限公司 | Countercurrent flow esterification reactor for preparing biodiesel and method thereof |
| CN101492603B (en) * | 2008-01-23 | 2012-11-28 | 华中农业大学 | Method for producing biodiesel by using tallowseed oil and special solid catalyst thereof |
| CN101250425B (en) * | 2008-04-10 | 2011-11-02 | 中国寰球工程公司 | Method for preparing bio-diesel oil by employing annular-pipe reactor |
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| CN101560427B (en) * | 2009-05-27 | 2012-02-01 | 江苏高科石化股份有限公司 | Preparation method of biological lube base oil and preparation device thereof |
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| CN102703223B (en) * | 2012-05-31 | 2013-08-21 | 源华能源科技（福建）有限公司 | Process for preparing biodiesel by catalytic esterification and alcoholysis of gas-phase methanol |
| CN103031216A (en) * | 2013-01-09 | 2013-04-10 | 杨玉峰 | Pre-esterification process for producing biodiesel from illegal cooking oil |
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| CN103894168A (en) * | 2014-04-18 | 2014-07-02 | 厦门大学 | Magnesium oxide solid base catalyst as well as preparation method and application thereof |
| CN106147849B (en) * | 2015-04-21 | 2019-03-08 | 中国石油化工股份有限公司 | Two sections of heavy-oil slurry hydrogenation plants of one kind and method |
| CN106147848B (en) * | 2015-04-21 | 2019-03-08 | 中国石油化工股份有限公司 | Two sections of heavy-oil slurry hydrogenation plants of one kind and method |
| CN106147851B (en) * | 2015-04-23 | 2018-08-28 | 中国石油化工股份有限公司 | A kind of heavy-oil slurry hydrogenation reaction device and methods for using them |
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| CN105457461B (en) | 2015-12-29 | 2018-04-10 | 原初科技（北京）有限公司 | A kind of carbon dioxide absorption and the device and method that mineralizes |
| CN106281727B (en) * | 2016-09-14 | 2019-10-18 | 浙江工业大学 | A kind of novel ester exchange reaction device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1279663A (en) * | 1997-11-24 | 2001-01-10 | 能源环境技术股份有限公司 | Method and equipment for producing fatty acid methyl ester |
| RO119828B1 (en) * | 2002-07-04 | 2005-04-29 | Ion Oprescu | Process and installation for producing high purity esters of fatty acids |
-
2006
- 2006-12-07 CN CNB2006101299196A patent/CN100412170C/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1279663A (en) * | 1997-11-24 | 2001-01-10 | 能源环境技术股份有限公司 | Method and equipment for producing fatty acid methyl ester |
| RO119828B1 (en) * | 2002-07-04 | 2005-04-29 | Ion Oprescu | Process and installation for producing high purity esters of fatty acids |
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