CN107057838B - Microalgae combined treatment device based on vapor recompression and heat exchange integration - Google Patents
Microalgae combined treatment device based on vapor recompression and heat exchange integration Download PDFInfo
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- CN107057838B CN107057838B CN201710394218.3A CN201710394218A CN107057838B CN 107057838 B CN107057838 B CN 107057838B CN 201710394218 A CN201710394218 A CN 201710394218A CN 107057838 B CN107057838 B CN 107057838B
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- 230000010354 integration Effects 0.000 title claims abstract description 8
- 241000195493 Cryptophyta Species 0.000 claims abstract description 32
- 239000004519 grease Substances 0.000 claims abstract description 23
- 239000002904 solvent Substances 0.000 claims abstract description 21
- 238000001035 drying Methods 0.000 claims abstract description 19
- 238000000605 extraction Methods 0.000 claims abstract description 19
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 238000005336 cracking Methods 0.000 claims description 9
- 239000011877 solvent mixture Substances 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 4
- 239000002910 solid waste Substances 0.000 claims description 4
- 239000003921 oil Substances 0.000 description 16
- 239000007789 gas Substances 0.000 description 14
- 238000000034 method Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000003225 biodiesel Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 235000013339 cereals Nutrition 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 208000016253 exhaustion Diseases 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000003306 harvesting Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 238000005382 thermal cycling Methods 0.000 description 1
- 238000005809 transesterification reaction Methods 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/02—Pretreatment
- C11B1/04—Pretreatment of vegetable raw material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0292—Treatment of the solvent
- B01D11/0296—Condensation of solvent vapours
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/10—Production of fats or fatty oils from raw materials by extracting
- C11B1/104—Production of fats or fatty oils from raw materials by extracting using super critical gases or vapours
-
- 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
- C10L2200/00—Components of fuel compositions
- C10L2200/04—Organic compounds
- C10L2200/0461—Fractions defined by their origin
- C10L2200/0469—Renewables or materials of biological origin
- C10L2200/0484—Vegetable or animal oils
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/544—Extraction for separating fractions, components or impurities during preparation or upgrading of a fuel
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- General Chemical & Material Sciences (AREA)
- Extraction Or Liquid Replacement (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to the technical field of microalgae high-energy-efficiency treatment, in particular to a microalgae combined treatment device based on integration of vapor recompression and heat exchange, which comprises three systems, namely microalgae drying, grease extraction and solvent recovery, wherein the two systems are respectively provided with vapor recompression steps. The invention compresses the gas at the top end of the dryer, and the gas enters the second-stage heat exchanger to exchange heat with wet algae, and simultaneously, the energy exchange is carried out by utilizing the dried algae and the wet algae. Vapor recompression is carried out in the microalgae drying process, so that the energy efficiency is improved, the energy is exchanged with wet algae, and meanwhile, the exchange of the energy of the wet algae and the dry algae is realized; and in the solvent recovery stage, the energy of the gas flow at the top of the fractionating column is recovered by recovering the energy of the top of the fractionating column and introducing the gas flow into a compressor, so that the energy efficiency is improved, and a preheater and a reboiler are omitted.
Description
Technical Field
The invention relates to the technical field of microalgae high-energy-efficiency treatment, in particular to a microalgae combined treatment device based on vapor recompression and heat exchange integration.
Background
The progressive exhaustion of fossil fuels and the resulting greenhouse effect, etc. have prompted the rapid development of renewable energy sources. The bioenergy has sustainability, environmental friendliness and good adaptability, and in addition, the bioenergy can reduce CO 2 Is a kind of dischargeA good alternative to fossil fuels.
Bioenergy can be divided into three generations according to the raw materials. The first generation of bioenergy sources, the raw materials of which include sugar, cereal, oil crop seeds, etc., but it is impractical to utilize bioenergy sources that use edible biomass as a raw material due to their occupation of cultivated land; the second-generation bioenergy raw material is non-edible cellulose biomass, including agricultural and forestry waste and non-edible biomass, but a series of technical problems still exist in the utilization of the second-generation bioenergy; the third generation biological energy source material is mainly microalgae. Under proper environmental conditions, the microalgae can produce 50 per unit mass of dry algae ～ 70% of grease. However, prior to commercial production, technical and economic problems must be solved. The complex production routes of microalgae, including cultivation, harvesting, drying, oil extraction and transesterification, result in high production costs of biodiesel.
Drying and grease extraction are the most energy-consuming parts of a series of grease extraction production routes, and occupy about 90% of energy. In the traditional process, only the solvent at the top of the fractionating column is recovered during oil extraction, and the heat energy is not fully utilized; the drying system only uses the dried algae to reduce the energy requirement of the preheating process by exchanging energy with wet algae, and does not fully use the heat energy. Although thermal cycling techniques in microalgae drying and techniques for oil extraction with organic solvents have been continuously developed, comprehensive energy assessment for microalgae drying and oil extraction is still lacking.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a microalgae combined treatment device based on vapor recompression and heat exchange integration.
The technical scheme of the invention is that the microalgae combined treatment device based on vapor recompression and heat exchange integration comprises three systems, namely microalgae drying, grease extraction and solvent recovery, wherein the two systems are respectively provided with vapor recompression steps;
the microalgae drying system comprises an evaporator, wherein an inlet pipeline of the evaporator is connected with two sections of heat exchangers and an inlet pump which are connected in series, an outlet pipeline at the top of the evaporator is connected to an inlet of a separator III, an outlet pipeline at the bottom of the evaporator and an outlet pipeline at the bottom of the separator III are connected to an inlet of a mixer together, an outlet pipeline at the top of the separator III is connected to an inlet of a compressor, an outlet pipeline of the compressor is communicated to a cooler connected in series after heat exchange in a second section of heat exchanger in the two sections of heat exchangers, and an outlet pipeline of the mixer is communicated to a first section of heat exchanger in the two sections of heat exchangers and then is connected to the grease extraction system;
the grease extraction system comprises a mixer, wherein dry algae and solvent are collected in the mixer, an outlet pipeline of the mixer is sequentially connected with a cracking reactor, a separator I, a heat exchanger I and a fractionating column, and an outlet pipe at the bottom of the fractionating column is connected with the separator II through a heat exchanger II to separate algae oil;
wherein, solvent recovery system includes connecting compressor and shunt on the top outlet pipe of fractionating column, and the shunt divides into two heat exchange: one path of the oil is pumped into the heat exchanger I, the other path of the oil is connected with the heat exchanger II, the heat exchanger I and the heat exchanger II are respectively used for heating the mixture before the fractionating column and the oil/solvent mixture at the bottom of the fractionating column, and the two paths of the oil/solvent mixtures are converged to an inlet of the mixer after heat exchange.
The top of the cracking reactor is provided with an exhaust gas discharge port.
The bottom of the separator I is provided with a solid waste discharge pipe.
The heat exchanger I is connected to the inlet of the mixer via a cooler.
Compared with the prior art, the invention has the advantages that:
1. compared with the traditional microalgae drying system, the invention carries out vapor recompression on the gas at the top end of the dryer, enters the second-stage heat exchanger to exchange heat with wet algae, and simultaneously carries out energy exchange by using the dried microalgae and the wet microalgae. Vapor recompression is carried out in the microalgae drying process, so that the energy efficiency is improved, the energy is exchanged with wet algae, and meanwhile, the exchange of the energy of the wet algae and the dry algae is realized; and in the solvent recovery stage, the energy of the gas flow at the top of the fractionating column is recovered by recovering the energy of the top of the fractionating column and introducing the gas flow into a compressor, so that the energy efficiency is improved, and a preheater and a reboiler are omitted.
2. The microalgae grease extraction system of the invention performs vapor recompression on the distillate obtained in the distillation column, one part of recompressed air flow returns to the heat exchanger and the grease/solvent mixture exchanges energy, and the other part of recompressed air flow enters the heat exchanger for heating bottom air flow (essential oil).
3. The invention has simple structure and easy realization, saves 35.3 percent of energy (the energy consumption of the whole system of the traditional process is 14.55MW, the energy consumption of the improved system is 9.43 MW) compared with the traditional process, reduces the operation cost well in the whole process, and realizes the comprehensive analysis of microalgae drying and grease extraction.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Reference numerals: 1-inlet pump, 2-first section heat exchanger, 3-second heat exchanger, 4-evaporator, 5-separator III, 7-compressor, 8-cooler, 6, 9-mixer, 8, 10-cooler, 11-cracking reactor, 12-separator I, 13-heat exchanger I, 14-fractionation column, 15-separator II, 16-compressor, 17-diverter, 18-heat exchanger II.
Detailed Description
The technical scheme of the invention is further described below with reference to the accompanying drawings.
As shown in figure 1, the microalgae combined treatment device based on vapor recompression and heat exchange integration comprises three systems of microalgae drying I, grease extraction II and solvent recovery III, wherein the two systems of microalgae drying I and solvent recovery III are provided with vapor recompression steps;
the microalgae drying system comprises an evaporator 4, two sections of heat exchangers 2 and 3 connected in series and an inlet pump 1 are connected to an inlet pipeline of the evaporator 4, an outlet pipeline at the top of the evaporator 4 is connected with an inlet of a separator III 5, an outlet pipeline at the bottom of the evaporator 4 and an outlet pipeline at the bottom of the separator III 5 are connected to an inlet of a mixer 6 together, an outlet pipeline at the top of the separator III 5 is connected to an inlet of a compressor 7, an outlet pipeline of the compressor 7 is communicated to a serially connected cooler 8 after heat exchange in a second section of heat exchanger 3 in the two sections of heat exchangers, compressed water is discharged after condensation, and an outlet pipeline of the mixer 6 is communicated to a first section of heat exchanger 2 in the two sections of heat exchangers for heat exchange to obtain dry algae and is connected to a grease extraction system through an outlet pump pipeline.
The grease extraction system comprises a mixer 9, wherein dry algae and solvent are gathered into the mixer 9, an outlet pipeline of the mixer 9 is sequentially connected with a cracking reactor 11, a separator I12, a heat exchanger I13 and a fractionating column 14, and an outlet pipe at the bottom of the fractionating column 14 is connected with a separator II 15 through a heat exchanger II 18 to separate algae oil; the cracking reactor 11 extracts grease from microalgae and conveys the grease to the separator I12, solid waste is separated and discharged from the bottom of the separator I12, and an outlet pipe in the middle of the separator I12 is connected to an inlet of the fractionating column 14 through a heat exchanger I13; the fractionating column 14 separates the chemical solvent from the microalgae grease, and recovers the chemical solvent; the top of the cracking reactor 11 discharges waste gas; a compressor 16 is arranged on an outlet pipe at the top of the fractionating column 14, a diverter 17 is connected to an outlet pipe of the compressor 16, and the compressor is respectively pumped into a heat exchanger I13 and a heat exchanger II 18 for heat exchange, wherein the heat exchanger I13 and the heat exchanger II 18 respectively heat a mixture before the fractionating column 14 and a grease/solvent mixture at the bottom of the fractionating column 14; the heat exchanger I13 merges via a cooler 10 into the mixer 9.
The solvent recovery system comprises a compressor 16 and a splitter 17 connected to the top outlet pipe of the fractionating column 14, the splitter 17 splitting into two heat exchanges: one path of the oil is pumped into the heat exchanger I13, the other path of the oil is connected with the heat exchanger II 18, the heat exchanger I13 and the heat exchanger II 18 are respectively used for heating the mixture before the fractionating column 14 and the oil/solvent mixture at the bottom of the fractionating column 14, and the two paths of the oil/solvent mixtures are converged to the inlet of the mixer 9 after heat exchange.
The working process of the invention is as follows:
the wet algae enters the microalgae drying system through the inlet pump 1, firstly, the wet algae exchanges with the dry algae in the first-stage heat exchanger 2 to obtain energy, compared with the prior art, as shown in figure 1, the wet algae exchanges with the high-pressure high-temperature gas phase separated in the separator 4 in the second-stage heat exchanger 3 to obtain heat, and the heat enters the evaporator 4 after the two-step heat exchange. The bottom discharged dry algae separated by the steam at the top outlet of the evaporator 4 through the separator 5 and the bottom discharged dry algae of the evaporator 4 are mixed in the mixer 6 and conveyed into the first section heat exchanger 2 to supply heat energy to wet algae; the top gas phase separated by the separator 5 enters a compressor 7, wet algae is heated in the second section heat exchanger 3 after the available energy efficiency is improved, and residual water vapor is discharged and compressed into water through a cooler 8; the dry algae discharged from the bottom of the evaporator 4 returns to the first heat exchanger 2 and the wet algae to exchange heat, and then is conveyed into a mixer 9 of the grease extraction system through an outlet pump 9.
The dry algae is transported to a mixer 9 through a pump, is uniformly mixed with an external solvent and a solvent subjected to heat exchange by a heat exchanger I13 and a heat exchanger II 18 of top recovered gas separated by a fractionating column 14, enters a cracking reactor 11 for reaction, and is discharged from waste gas, and then enters a separator I12 for discharging solid waste; the heat is absorbed by the heat exchange between the heat exchanger I13 and the gas from the compressor 16, the gas enters the fractionating column 14, the top gas flow separated by the fractionating column 14 is recovered, the gas is compressed into high-temperature and high-pressure gas by the compressor 16 and is split by the splitter 17, one part of the gas is supplied to the heat exchanger I13 by a pump for heating the grease/solvent mixture entering the fractionating column 14, and the other part of the gas is supplied to the heat exchanger II 18 for heating the grease/solvent coming out of the bottom of the fractionating column 14; the bottom of the fractionating column 14 flows out through a separator II 15 to extract the algae oil after solvent recovery, and the top air flow flows back into the fractionating column 14 for continuous fractionating operation.
The present invention is not limited to the above-described embodiments, and variations in operation and control modes made by those skilled in the art without departing from the form of the system of the present invention are within the scope of the present invention.
Claims (1)
1. The microalgae combined treatment device based on vapor recompression and heat exchange integration comprises three systems, namely microalgae drying, grease extraction and solvent recovery, and is characterized in that the microalgae drying and solvent recovery systems are both provided with vapor recompression steps;
the microalgae drying system comprises an evaporator (4), two sections of heat exchangers (2), (3) and an inlet pump (1) which are connected in series are connected to an inlet pipeline of the evaporator (4), a top outlet pipeline of the evaporator (4) is connected to an inlet of a separator III (5), a bottom outlet pipeline of the evaporator (4) and a bottom outlet pipeline of the separator III (5) are connected to an inlet of a mixer I (6), a top outlet pipeline of the separator III (5) is connected to an inlet of a compressor I (7), an outlet pipeline of the compressor I (7) is communicated to a cooler I (8) connected in series after heat exchange in a second section of heat exchanger (3) in the two sections of heat exchangers, and an outlet pipeline of the mixer I (6) is communicated to a first section of heat exchanger (2) in the two sections of heat exchangers and then is connected to the grease extraction system;
the grease extraction system comprises a mixer II (9), wherein dry algae and solvent are introduced into the mixer II (9), an outlet pipeline of the mixer II (9) is sequentially connected with a cracking reactor (11), a separator I (12), a heat exchanger I (13) and a fractionating column (14), and an outlet pipe at the bottom of the fractionating column (14) is connected with the separator II (15) through a heat exchanger II (18) to separate algae oil;
wherein the solvent recovery system comprises a compressor II (16) and a splitter (17) connected to the top outlet pipe of the fractionating column (14), and the splitter (17) splits into two heat exchanges: one path of the oil is pumped into a heat exchanger I (13) and the other path of the oil is connected with a heat exchanger II (18), the heat exchanger I (13) and the heat exchanger II (18) are respectively used for heating the mixture before the fractionating column (14) and the oil/solvent mixture at the bottom of the fractionating column (14), and the two paths of the oil/solvent mixtures are converged to an inlet of the mixer II (9) after heat exchange;
the heat exchanger I (13) is connected to the inlet of the mixer II (9) through a cooler II (10);
the top of the cracking reactor (11) is provided with an exhaust gas discharge port;
the bottom of the separator I (12) is provided with a solid waste discharge pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201710394218.3A CN107057838B (en) | 2017-05-28 | 2017-05-28 | Microalgae combined treatment device based on vapor recompression and heat exchange integration |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710394218.3A CN107057838B (en) | 2017-05-28 | 2017-05-28 | Microalgae combined treatment device based on vapor recompression and heat exchange integration |
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| Publication Number | Publication Date |
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| CN107057838A CN107057838A (en) | 2017-08-18 |
| CN107057838B true CN107057838B (en) | 2023-12-08 |
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| CN1351109A (en) * | 2000-10-31 | 2002-05-29 | 法国石油公司 | Method for inversion of olefins by heat absorption, use thereof and apparatus therefor |
| CN200974829Y (en) * | 2006-12-01 | 2007-11-14 | 华南理工大学 | Auxiliary fractionating tower |
| CN101358143A (en) * | 2008-08-28 | 2009-02-04 | 天津大学 | Ethylene quenching apparatus and compressing energy-saving technique |
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| CN102533437A (en) * | 2012-03-09 | 2012-07-04 | 广西大学 | Method for extracting microalgae grease through supercritical CO2 isobaric variable temperature technology |
| CN102939397A (en) * | 2010-01-22 | 2013-02-20 | 莫利康普矿物有限责任公司 | Hydrometallurgical process and method for recovering metals |
| CN104987885A (en) * | 2015-07-09 | 2015-10-21 | 陕西美斯林能源科技研究院 | Technology and device for producing national standard oil through fischer-tropsch synthesis oil and coal tar through hydrogenation |
| CN105647652A (en) * | 2016-02-29 | 2016-06-08 | 薛晶 | Microalgae biodiesel production device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9284502B2 (en) * | 2012-01-27 | 2016-03-15 | Saudi Arabian Oil Company | Integrated solvent deasphalting, hydrotreating and steam pyrolysis process for direct processing of a crude oil |
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2017
- 2017-05-28 CN CN201710394218.3A patent/CN107057838B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1351109A (en) * | 2000-10-31 | 2002-05-29 | 法国石油公司 | Method for inversion of olefins by heat absorption, use thereof and apparatus therefor |
| CN200974829Y (en) * | 2006-12-01 | 2007-11-14 | 华南理工大学 | Auxiliary fractionating tower |
| CN101358143A (en) * | 2008-08-28 | 2009-02-04 | 天津大学 | Ethylene quenching apparatus and compressing energy-saving technique |
| CN101748053A (en) * | 2008-12-17 | 2010-06-23 | 新奥科技发展有限公司 | Reaction system for cultivating microalgae and preparing bioenergy |
| CN102939397A (en) * | 2010-01-22 | 2013-02-20 | 莫利康普矿物有限责任公司 | Hydrometallurgical process and method for recovering metals |
| CN102533437A (en) * | 2012-03-09 | 2012-07-04 | 广西大学 | Method for extracting microalgae grease through supercritical CO2 isobaric variable temperature technology |
| CN104987885A (en) * | 2015-07-09 | 2015-10-21 | 陕西美斯林能源科技研究院 | Technology and device for producing national standard oil through fischer-tropsch synthesis oil and coal tar through hydrogenation |
| CN105647652A (en) * | 2016-02-29 | 2016-06-08 | 薛晶 | Microalgae biodiesel production device |
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| CN107057838A (en) | 2017-08-18 |
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