CN109913256B - Method and system for preparing fuel by using high-acid-value biological grease - Google Patents
Method and system for preparing fuel by using high-acid-value biological grease Download PDFInfo
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- 239000002253 acid Substances 0.000 title claims abstract description 132
- 238000000034 method Methods 0.000 title claims abstract description 55
- 239000004519 grease Substances 0.000 title claims abstract description 36
- 239000000446 fuel Substances 0.000 title claims abstract description 22
- 238000004227 thermal cracking Methods 0.000 claims abstract description 53
- 230000003197 catalytic effect Effects 0.000 claims abstract description 36
- 239000003921 oil Substances 0.000 claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims description 62
- 238000004523 catalytic cracking Methods 0.000 claims description 59
- 238000004821 distillation Methods 0.000 claims description 52
- 238000006392 deoxygenation reaction Methods 0.000 claims description 38
- 239000003054 catalyst Substances 0.000 claims description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 229910001868 water Inorganic materials 0.000 claims description 28
- 238000010438 heat treatment Methods 0.000 claims description 26
- 230000008569 process Effects 0.000 claims description 24
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 20
- 239000001257 hydrogen Substances 0.000 claims description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 17
- 239000000203 mixture Substances 0.000 claims description 13
- 238000005292 vacuum distillation Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 10
- 235000021588 free fatty acids Nutrition 0.000 claims description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 8
- 239000001569 carbon dioxide Substances 0.000 claims description 8
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 8
- 239000002699 waste material Substances 0.000 claims description 8
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 7
- 150000001336 alkenes Chemical class 0.000 claims description 7
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 7
- 229930195729 fatty acid Natural products 0.000 claims description 7
- 239000000194 fatty acid Substances 0.000 claims description 7
- 150000004665 fatty acids Chemical class 0.000 claims description 7
- 239000003502 gasoline Substances 0.000 claims description 6
- 241001465754 Metazoa Species 0.000 claims description 5
- 150000002576 ketones Chemical class 0.000 claims description 5
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- 229910052976 metal sulfide Inorganic materials 0.000 claims description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 150000002191 fatty alcohols Chemical class 0.000 claims description 4
- 230000000813 microbial effect Effects 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 4
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims description 4
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- 235000013311 vegetables Nutrition 0.000 claims description 4
- 239000002994 raw material Substances 0.000 abstract description 9
- 238000007670 refining Methods 0.000 abstract description 6
- 239000010779 crude oil Substances 0.000 abstract description 4
- 235000019198 oils Nutrition 0.000 description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 9
- 238000005984 hydrogenation reaction Methods 0.000 description 9
- 239000001301 oxygen Substances 0.000 description 9
- 229910052760 oxygen Inorganic materials 0.000 description 9
- 239000010802 sludge Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 235000015112 vegetable and seed oil Nutrition 0.000 description 5
- 239000002028 Biomass Substances 0.000 description 4
- 239000003225 biodiesel Substances 0.000 description 4
- 239000008158 vegetable oil Substances 0.000 description 4
- 239000012075 bio-oil Substances 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
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- 238000006114 decarboxylation reaction Methods 0.000 description 3
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- 239000003208 petroleum Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 2
- 230000006324 decarbonylation Effects 0.000 description 2
- 238000006606 decarbonylation reaction Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
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- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 241000221089 Jatropha Species 0.000 description 1
- 235000019482 Palm oil Nutrition 0.000 description 1
- 235000019484 Rapeseed oil Nutrition 0.000 description 1
- 235000019486 Sunflower oil Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000014121 butter Nutrition 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 239000004359 castor oil Substances 0.000 description 1
- 235000019438 castor oil Nutrition 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000008162 cooking oil Substances 0.000 description 1
- 235000012343 cottonseed oil Nutrition 0.000 description 1
- 239000002385 cottonseed oil Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000003635 deoxygenating effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 235000021323 fish oil Nutrition 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- ZEMPKEQAKRGZGQ-XOQCFJPHSA-N glycerol triricinoleate Natural products CCCCCC[C@@H](O)CC=CCCCCCCCC(=O)OC[C@@H](COC(=O)CCCCCCCC=CC[C@@H](O)CCCCCC)OC(=O)CCCCCCCC=CC[C@H](O)CCCCCC ZEMPKEQAKRGZGQ-XOQCFJPHSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 235000014593 oils and fats Nutrition 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000004006 olive oil Substances 0.000 description 1
- 235000008390 olive oil Nutrition 0.000 description 1
- 239000002540 palm oil Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000003549 soybean oil Substances 0.000 description 1
- 235000012424 soybean oil Nutrition 0.000 description 1
- 239000002600 sunflower oil Substances 0.000 description 1
- 239000003760 tallow Substances 0.000 description 1
- 235000019871 vegetable fat Nutrition 0.000 description 1
Images
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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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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a method and a system for preparing fuel by using high-acid-value biological grease, which can perform thermal cracking deoxidation, catalytic hydrodeoxygenation and triple deoxidation steps and treat the high-acid-value biological grease. By utilizing the method and the system, the biological oil raw material with high acid value can be gradually deoxidized to reduce the acid value, and clean fuel with the fuel component equivalent to that obtained by crude oil refining or direct hydrodeoxygenation of the biological oil can be prepared.
Description
Technical Field
The invention belongs to the technical field of energy regeneration, and particularly relates to a method and a system for preparing fuel by using high-acid-value biological grease.
Background
As for the direct hydrogenation technology, WO2009/039347 teaches a technology for producing diesel components from bio-renewable feedstock (bionewable fed stock) in a two-step process of hydrodeoxygenation and hydroisomerization. US2006/0207166 teaches a technique of simultaneous hydrodeoxygenation and hydroisomerization. A common drawback of these techniques is the poor stability of the catalyst and the high hydrogen consumption of the process, which causes problems of corrosion of the equipment, especially for the processing of vegetable oils and animal fats with high oxygen content and high acid number.
In particular, direct hydrogenation techniques are limited by the content of free fatty acids in the feedstock, and so far the literature of the prior art only discloses the direct hydrotreatment of up to 15% of free fatty acids to produce hydrocarbon fuels (Yanyong Liu et al, chem. lett.2009,38,552).
Meanwhile, other technologies for preparing biodiesel from biological grease exist in the prior art, for example, US2006/0186020 discloses a method for co-refining vegetable oil and crude oil, wherein the content of the vegetable oil is between 1 and 75 percent, but the method does not use the vegetable oil alone. And the co-refining has problems in that the low-temperature fluidity of normal paraffin components generated during the hydrogenation process is poor, the low-temperature use performance of the final diesel product may be affected, and the desulfurization refining effect of petroleum diesel may be affected.
In summary, in the prior art, although there are many routes and research results for processing and preparing fuel by using high-acid value biological grease as raw material, the problems of low catalyst stability, corrosion of device, high hydrogen consumption and the like still exist.
Meanwhile, other technologies for preparing biodiesel by using biological grease exist in the prior art, for example, CN102492455A proposes a dual deoxidation technology of catalytic cracking deoxidation and catalytic hydrodeoxygenation. The technology is limited by the continuous change of raw oil components, once the raw oil components become heavier, the tower bottom of the catalytic cracking deoxygenation tower needs higher temperature to ensure certain yield of tower top fraction, but the problem of serious polymerization or coking of heavy oil at the tower bottom can be caused at the same time.
Disclosure of Invention
In this summary, concepts in a simplified form are introduced that are further described in the detailed description. This summary of the invention is not intended to identify key features or essential features of the claimed subject matter, nor is it intended to be used as an aid in determining the scope of the claimed subject matter.
In order to overcome the problems, the invention provides a method for preparing fuel by using high-acid-value biological grease. The process preferably enables the production of high quality biomass fuels suitable as diesel blending components, which are comparable to those obtained from crude oil refining.
Specifically, the invention provides a method for preparing fuel by using high-acid-value biological grease, which takes the high-acid-value biological grease as a raw material, and the method comprises the following steps:
(a) carrying out thermal cracking deoxidation reaction on the high-acid-value biological grease under the heating condition;
(b) carrying out reduced pressure distillation on the product obtained in the step (a), and separating out water, a high-acid-value fraction, a low-acid-value fraction and heavy components;
(c) in the presence of a catalytic cracking deoxidation catalyst, carrying out catalytic cracking deoxidation reaction on the high-acid-value fraction obtained in the step (b) under the heating condition, and separating water and non-condensable gas;
(d) subjecting the mixture of the product obtained in step (c) and the low acid number fraction obtained in step (b) to catalytic hydrodeoxygenation with hydrogen in the presence of a hydrodeoxygenation catalyst under heated conditions.
According to the actual application requirement, the method can further comprise the following steps: (e) fractionating the product of step (d) to obtain a gasoline component, a diesel component and a heavy component at >365 ℃; wherein the heavier components >365 ℃ may be mixed with the high acid number fraction of step (b) as part of the feed for the catalytic cracking deoxygenation reaction.
According to another aspect of the present invention, there is provided a system for preparing fuel using high acid value bio-grease, comprising:
the thermal cracking reactor is used for receiving the high-acid-value biological grease and carrying out thermal cracking deoxidation reaction on the high-acid-value biological grease under the heating condition;
the reduced pressure distillation tower is connected with the thermal cracking reactor, receives a product obtained by thermal cracking deoxidation reaction, performs reduced pressure distillation, and separates water, a high acid value fraction, a low acid value fraction and a heavy component;
the catalytic cracking deoxidation reactor is connected with the reduced pressure distillation tower, and is used for carrying out catalytic cracking deoxidation reaction on the high-acid-value fraction obtained by reduced pressure distillation in the presence of a catalytic cracking deoxidation catalyst under the heating condition to separate water and non-condensable gas;
and a hydrofining reaction tower which receives and mixes the product from the catalytic cracking and deoxygenation reactor and the low acid value fraction from the reduced pressure distillation tower, and performs catalytic hydrodeoxygenation reaction with hydrogen under the heating condition in the presence of a hydrodeoxygenation catalyst.
The system can also comprise an atmospheric distillation tower which is connected with the hydrofining reaction tower and is used for fractionating the products of the hydrofining reaction tower according to the requirements of practical application. Further, the system may further include a preheater coupled to the thermal cracking reactor for preheating the high acid value biological oil entering the thermal cracking reactor.
The method and the system use thermal cracking deoxidation, catalytic hydrodeoxygenation and triple deoxidation steps to treat the high-acid-value biological oil, preferably waste high-acid-value biological oil. In addition, the thermal cracking deoxidation, the catalytic cracking deoxidation and the catalytic hydrodeoxygenation in the present invention can be operated not only continuously but also separately, that is, continuously or intermittently, depending on the operating conditions in practical use. In the invention, the generated waste residues and the non-condensable gas can be comprehensively utilized for heating, so that the whole production process is more energy-saving and environment-friendly.
Drawings
The following drawings of the invention are included to provide a further understanding of the invention. The drawings illustrate embodiments of the invention and, together with the description, serve to explain the principles of the invention.
FIG. 1 depicts one embodiment of a system according to the present invention.
Description of the main component symbols:
1. preheater
2. Thermal cracking reactor
3. Vacuum distillation tower
4. Catalytic cracking deoxidation reactor
5. Hydrofining reaction tower
6. Atmospheric distillation tower
Detailed Description
In the following description, numerous specific details are set forth in order to provide a more thorough understanding of the present invention. It will be apparent, however, to one skilled in the art, that the present invention may be practiced without one or more of these specific details. In other instances, some features known in the art are not described.
The pressures described herein are gauge pressures.
The invention relates to a method for preparing fuel by using high-acid-value biological grease, which comprises the following steps: (a) carrying out thermal cracking deoxidation reaction on the high-acid-value biological grease under the heating condition;
(b) carrying out reduced pressure distillation on the product obtained in the step (a), and separating out water, a high-acid-value fraction, a low-acid-value fraction and heavy components;
(c) in the presence of a catalytic cracking deoxidation catalyst, carrying out catalytic cracking deoxidation reaction on the high-acid-value fraction obtained in the step (b) under the heating condition, and separating water and non-condensable gas;
(d) subjecting the mixture of the product obtained in step (c) and the low acid number fraction obtained in step (b) to catalytic hydrodeoxygenation with hydrogen in the presence of a hydrodeoxygenation catalyst under heating.
The invention adopts a thermal cracking deoxidation, a catalytic hydrogenation deoxidation and a triple deoxidation process. The method is characterized in that a technology combining thermal cracking and reduced pressure distillation is adopted to treat the high-acid-value biological grease, partial oxygen elements in the raw materials can be removed in the process, the acid value, the density and the viscosity of the raw materials are reduced, and the biological grease is divided into four parts, namely water, high-acid-value fractions, low-acid-value fractions and heavy components. The low acid value fraction can be directly used as one of the raw materials for catalytic hydrodeoxygenation reaction, while the high acid value fraction can be further deprived of oxygen element by catalytic cracking deoxygenation reaction to reduce the acid value to a lower level (for example <50 mgKOH/g). Finally, the residual oxygen element is removed through catalytic hydrodeoxygenation reaction. Because hydrogen is not needed in the steps of thermal cracking deoxidation and catalytic cracking deoxidation and most of oxygen elements are removed, the hydrogen consumption can be greatly reduced in the subsequent catalytic hydrodeoxygenation step, and the hydrogenation operation condition is milder than that of the direct hydrogenation of biological grease.
In the thermal cracking deoxidation step, partial fatty acid is subjected to decarboxylation, degradation, isomerization and other reactions at high temperature to form alkane, olefin, ketone, water and CO2CO, hydrogen, methane, ethane, etc. Thereby reducing the acid value, density and viscosity and being beneficial to the next treatment of the grease.
In the step of catalytic cracking deoxidation and acid value reduction, the residual fatty acid in the high acid value fraction removes partial oxygen through decarbonylation or decarboxylation to generate CO2、CO、H2O and alkanes, alkenes. The acid value can be reduced to a lower level by this step (for example<50mgKOH/g)。
In the step of catalytic hydrodeoxygenation, triglyceride undergoes hydrogenation saturation, hydrogenation decarboxylation, hydrogenation decarbonylation and hydrogenation deoxygenation reactions to produce normal alkane. The hydrodeoxygenation reaction can further remove oxygen-containing fractions which are not removed in the process, and simultaneously saturate olefins generated in the thermal cracking deoxygenation-catalytic cracking deoxygenation process to obtain a product with high stability.
The fuel produced by the present invention is generally referred to as biomass fuel, and means a solid, liquid, or gas composed of or extracted from biomass, and the so-called biomass means an organic living body or a product of metabolism of the organic living body. In a preferred embodiment, the biodiesel of the present invention is comparable in composition to petroleum diesel obtained by refining petrochemical feedstocks (e.g., crude oil), is highly compatible, is well-regulated, and has properties and application ranges comparable to petroleum diesel.
According to a preferred embodiment of the present invention, steps (a), (b) and (d) may be operated continuously and step (c) may be operated continuously or batchwise.
According to a preferred embodiment of the present invention, the batch operation of step (c) may employ a multiple still cycle reaction.
According to a preferred embodiment of the present invention, the continuous operation of step (c) may employ a continuous catalytic distillation reaction.
The method is mainly based on three steps of thermal cracking deoxidation, catalytic cracking deoxidation and catalytic hydrogenation deoxidation, and the combination of the three steps is very flexible, so that the method not only can be operated continuously, but also can be operated separately. Specifically, the first reaction zone in which the thermal cracking deoxygenation reaction (step (a)) and the vacuum distillation (step (b)) occur, the second reaction zone in which the catalytic cracking deoxygenation reaction (step (c)) occurs, and the third reaction zone in which the catalytic hydrodeoxygenation reaction (step (d)) occurs may be operated continuously or intermittently, respectively, depending on the actual operating conditions.
In industrial applications, the thermal cracking deoxidation and reduced pressure distillation steps in the first reaction zone and the catalytic hydrodeoxygenation step in the third reaction zone are preferably operated continuously, which has the advantages of stable reaction conditions and stable products; while the catalytic cracking deoxygenation step in the second reaction zone may be operated either batchwise or continuously. For example, the catalytic cracking deoxidation step can adopt multi-distillation kettle circulation operation or continuous catalytic distillation operation. Preferably, the catalytic cracking deoxygenation step is operated using a continuous catalytic distillation.
According to a preferred embodiment of the invention, the high acid value biolipid may be of animal origin, vegetable origin, microbial origin or mixtures of the foregoing. The high acid value biological grease can be waste high acid value biological grease. The acid value of the high-acid-value biological oil can be more than or equal to 80mgKOH/g or the content of free fatty acid can be more than or equal to 40 percent. The free fatty acid is free fatty acid generated by biological grease.
The biological oil may comprise animal origin, vegetable origin, microbial origin, or mixtures of the foregoing. Industrial or inedible biological oils and fats can be used. The biological oil is rich in triglyceride and free fatty acid, and the chain length of the fatty acid is usually C12-C24, more than C16 and C18. Examples of biological oils include, by way of example and not limitation, rapeseed oil, soybean oil, palm oil, sunflower oil, cottonseed oil, jatropha oil, olive oil, castor oil, microalgal oil, tallow, lard, butter, poultry fat, fish oil, waste cooking oil. In one embodiment, vegetable fats and oils are preferred as the raw material.
According to a preferred embodiment of the present invention, the heating condition in step (a) may be 100 ℃ to 600 ℃.
According to a preferred embodiment of the present invention, the thermal cracking deoxidation of the high acid value biological oil and fat in the step (a) may be performed for 1 to 60 minutes.
According to a preferred embodiment of the present invention, the product of step (a) may comprise alkenes, alkanes, ketones, fatty acids, fatty alcohols, carbon monoxide, carbon dioxide, water.
According to a preferred embodiment of the present invention, the acid value of the high acid value fraction obtained in step (b) may be in the range of 80 to 120mgKOH/g, and the acid value of the low acid value fraction may be in the range of 10 to 50 mgKOH/g.
According to a preferred embodiment of the present invention, the product of step (b) may comprise water, a high acid number fraction, a low acid number fraction, heavy components, carbon dioxide, carbon monoxide.
According to a preferred embodiment of the invention, the heavy fraction of step (b) can be disposed of as waste or mixed with the feed as feed for step (a).
According to a preferred embodiment of the present invention, step (b) may be carried out at a pressure of-0.05 MPa to-0.3 MPa.
According to a preferred embodiment of the present invention, the reduced pressure distillation of step (b) may be carried out at a temperature ranging from 100 ℃ to 500 ℃.
According to a preferred embodiment of the present invention, the catalytic cracking deoxygenation catalyst of step (c) may be selected from alumina, molecular sieves, silicon carbide or mixtures thereof.
According to a preferred embodiment of the present invention, step (c) may be carried out at a temperature ranging from 100 ℃ to 500 ℃.
According to a preferred embodiment of the present invention, step (d) may be carried out at a temperature ranging from 200 ℃ to 400 ℃, the hydrogen partial pressure may be from 1MPa to 6MPa, and the volume space velocity may be 0.5h-1To 4.0h-1The hydrogen-oil volume ratio may be 200-.
According to a preferred embodiment of the present invention, the method of the present invention may further comprise: (e) fractionating the product of step (d) to obtain a gasoline component, a diesel component and a heavy component at >365 ℃.
According to a preferred embodiment of the invention heavy components >365 ℃ can be mixed with the high acid number fraction of step (b) as part of the feed for the catalytic cracking deoxygenation reaction.
According to a preferred embodiment of the present invention, the step (a) may further include a step of preheating the high acid value bio-oil.
According to a preferred embodiment of the invention, the hydrodeoxygenation catalyst is a supported metal catalyst or a metal sulphide.
According to a preferred embodiment of the present invention, the water and the non-condensable gases obtained after the continuous catalytic distillation reaction are separated are used as the raw materials for the catalytic hydrodeoxygenation reaction in step (d).
According to a preferred embodiment of the present invention, the acid value of the product of step (c) is <50 mgKOH/g.
The invention also relates to a system for preparing fuel by using the high-acid-value biological grease, which comprises the following components: the thermal cracking reactor 2 is used for receiving the high-acid-value biological grease and carrying out thermal cracking deoxidation reaction on the high-acid-value biological grease under the heating condition; a reduced pressure distillation tower 3 which is connected with the thermal cracking reactor 2, receives the product obtained by the thermal cracking deoxidation reaction, carries out reduced pressure distillation, and separates out water, a high acid value fraction, a low acid value fraction and heavy components; a catalytic cracking deoxidation reactor 4 connected with the reduced pressure distillation tower 3, and used for carrying out catalytic cracking deoxidation reaction on the high acid value fraction from the reduced pressure distillation tower in the presence of a catalytic cracking deoxidation catalyst under the heating condition, and separating water and non-condensable gas; and a hydrorefining reaction tower 5 which is connected with the catalytic cracking and deoxygenation reactor 4 and the reduced pressure distillation tower 3, receives and mixes the product from the catalytic cracking and deoxygenation reactor 4 and the low acid value fraction from the reduced pressure distillation tower 3, and performs catalytic hydrodeoxygenation reaction with hydrogen under the heating condition in the presence of a hydrodeoxygenation catalyst.
According to a preferred embodiment of the present invention, the catalytic cracking and deoxygenating reactor 4 may employ a multi-still or catalytic distillation column. More preferably, the catalytic cracking and deoxygenation reactor 4 is a catalytic distillation tower, and the overhead fraction and the bottom fraction obtained by subjecting the high acid value fraction from the vacuum distillation tower 3 to catalytic cracking and deoxygenation reaction in the catalytic distillation tower have lower acid values (for example, less than 50mgKOH/g), which meets the requirement of the subsequent catalytic hydrodeoxygenation step on the acid value of the feed. However, in some cases, embodiments of the present invention may also use multiple stills instead of a catalytic distillation column.
According to a preferred embodiment of the present invention, the heating condition in the thermal cracking reactor 2 may be 100 ℃ to 600 ℃, and the residence time of the high acid value bio-oil in the thermal cracking reactor 2 may be 1 to 60 minutes.
According to a preferred embodiment of the present invention, the products of the thermal cracking reactor 2 may include olefins, alkanes, ketones, fatty acids, fatty alcohols, carbon monoxide, carbon dioxide, water.
According to a preferred embodiment of the present invention, the acid value of the high acid value fraction obtained in the vacuum distillation column 3 may be in the range of 80 to 120mgKOH/g, and the acid value of the low acid value fraction may be in the range of 10 to 50 mgKOH/g.
According to a preferred embodiment of the present invention, the product of the vacuum distillation column 3 may comprise water, a high acid number fraction, a low acid number fraction, heavy components, carbon dioxide, carbon monoxide; preferably, the heavy components can be disposed of as waste or mixed with the feedstock as feedstock to the thermal cracking reactor 2.
According to a preferred embodiment of the present invention, the pressure in the reduced pressure distillation column 3 may be-0.05 MPa to-0.3 MPa, and the temperature may be 200 ℃ to 500 ℃.
According to a preferred embodiment of the present invention, the catalytic cracking deoxygenation catalyst may be selected from the group consisting of alumina, molecular sieves, silicon carbide or mixtures thereof.
According to a preferred embodiment of the present invention, the heating condition of the catalytic cracking and deoxygenation reactor 4 may be in the temperature range of 100 ℃ to 500 ℃.
According to a preferred embodiment of the present invention, the hydrodeoxygenation catalyst can be a supported metal catalyst or a metal sulphide.
According to a preferred embodiment of the present invention, the heating condition in the hydrofining reaction tower 5 may be 200 ℃ to 400 ℃, the hydrogen partial pressure may be 1MPa to 6MPa, and the volume space velocity may be 0.5h-1To 4.0h-1The hydrogen-oil volume ratio may be 200-.
According to a preferred embodiment of the present invention, the system may further comprise an atmospheric distillation column 6 connected to the hydrofinishing reactor column 5 for fractionating the product of the hydrofinishing reactor column 6 to obtain a gasoline component, a diesel component and heavier components >365 ℃.
According to a preferred embodiment of the invention, the heavy components >365 ℃ can be mixed with the high acid number fraction obtained in the vacuum distillation column 3 as part of the feed to the catalytic cracking deoxygenation reactor 4.
According to a preferred embodiment of the present invention, the system may further comprise a preheater 1 connected to the thermal cracking reactor 2 for preheating the high acid value bio-oil introduced into the thermal cracking reactor 2.
According to a preferred embodiment of the present invention, the acid value of the product of the catalytic cracking deoxygenation reactor 4 is <50 mgKOH/g.
An embodiment of the system of the present invention is further described with reference to fig. 1.
Injecting the high-acid value biological grease into a preheater 1 for gasification, and then carrying out thermal cracking deoxidation reaction in a thermal cracking reaction tower 2; then, the product obtained from the thermal cracking reaction tower 2 is sent to a reduced pressure distillation tower 3 for reduced pressure distillation, and the separated product comprises water, a high acid value fraction, a low acid value fraction and a heavy component; injecting the high-acid-value fraction obtained by reduced pressure distillation separation into a catalytic cracking and deoxygenation reactor 4, and carrying out catalytic deoxygenation reaction in the catalytic cracking and deoxygenation reactor 4; then, the low acid value fraction from the vacuum distillation column 3 and the product from the catalytic cracking and deoxygenation reactor 4 are mixed with hydrogen gas and reacted in a hydrorefining reaction column 5 equipped with a hydrodeoxygenation catalyst; and finally, sending the mixed fraction obtained from the hydrofining reaction tower 5 into an atmospheric distillation tower 6, fractionating to obtain a gasoline component, a diesel oil component and a heavy component at a temperature of more than 365 ℃, wherein the heavy component at the temperature of more than 365 ℃ can be mixed with the high-acid-value fraction from the reduced pressure distillation tower 3 to be used as a part of the feed of the catalytic cracking deoxygenation reactor 4.
The invention has the advantages that the acid value of the biological grease can be reduced to an operable level through the dual deoxidation process of thermal cracking deoxidation and catalytic cracking deoxidation, and then the hydrodeoxygenation reaction is carried out, the reaction conditions are mild (the hydrogen partial pressure is low, the reaction temperature is low), the catalyst stability is good, the hydrogen consumption is low, and the corrosion problem of the device can be avoided.
Example 1
Palm sludge oil is used as the raw material of the method.
The basic properties and distillation range of palm sludge oil are shown in table 1. Palm sludge oil is a solid at room temperature and, due to its too high acid number, cannot be processed using prior art direct hydroprocessing techniques (as mentioned above, the prior art teaches only direct hydroprocessing up to 15% of free fatty acids to produce hydrocarbon fuels). However, palm sludge oil may be processed using the method of the present invention.
TABLE 1 basic characteristics of palm sludge oil
Injecting palm sludge oil into a preheater for gasification, carrying out thermal cracking deoxidation reaction in a thermal cracking reaction tower, controlling the thermal cracking temperature to be between 100 and 600 ℃, introducing a certain amount of nitrogen as carrier gas, controlling the pressure at the top of the tower to be between 0 and 2MPa, and controlling the retention time of oil products in the reaction tower to be between 5 and 60 minutes. Next, the product obtained by thermal cracking deoxygenation was distilled under reduced pressure to separate water, a high acid value fraction (80 to 120mgKOH/g) and a low acid value fraction (10 to 50mgKOH/g) depending on the temperature of the fractions, and the results are shown in Table 2.
TABLE 2 product distribution by vacuum distillation after thermal cracking deoxygenation
As is clear from a comparison of tables 1 and 2, the oxygen contained in the feedstock oil can be removed in the form of water by the thermal cracking deoxygenation and reduced pressure distillation steps of the method of the present invention, thereby reducing the removal of oxygen in the subsequent treatment process and extending the life of the catalytic cracking deoxygenation catalyst and the hydrodeoxygenation catalyst.
Injecting the high-acid value fraction obtained by reduced pressure distillation separation into the tower kettle of a catalytic distillation tower, heating and gasifying, and then carrying out catalytic cracking deoxidation reaction in the catalytic distillation tower, wherein the tower kettle temperature of the catalytic distillation tower is controlled between 100 ℃ and 600 ℃, and the ratio of a catalytic cracking deoxidation catalyst to raw oil is controlled between 1 and 20 (weight ratio). The ratio of the top fraction to the bottom fraction of the catalytic distillation column is shown in Table 3.
TABLE 3 catalytic cracking deoxygenation product distribution
| Overhead fraction | Column bottom fraction | Water (W) | Non-condensable gas |
| 70％ | 24.2％ | 1.8％ | 4％ |
Then, the low acid value fraction separated by the vacuum distillation and the overhead fraction and bottom fraction of the catalytic distillation column were mixed with hydrogen gas, and then passed through a reaction column equipped with a hydrodeoxygenation catalyst to perform a reaction. The supported metal or metal sulfide is used as the hydrodeoxygenation catalyst. The remaining reaction conditions are shown in table 4, and the compositional analysis of the resulting clean fuel is shown in table 5.
TABLE 4 hydrodeoxygenation conditions
TABLE 5 composition analysis of clean fuels
As shown in Table 5, the acid value of the fraction obtained after the fraction obtained by the thermal cracking deoxidation and the catalytic cracking deoxidation of the palm sludge oil is further subjected to hydrodeoxygenation treatment is reduced to 0.43mgKOH/g, which is far lower than the standard value of the China biodiesel standard (BD 100). The clean fuel derived from palm sludge oil according to the process of the present invention is indeed an excellent diesel blending component.
The present invention has been illustrated by the above embodiments, but it should be understood that the above embodiments are for illustrative and descriptive purposes only and are not intended to limit the invention to the scope of the described embodiments. Furthermore, it will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that many variations and modifications may be made in accordance with the teachings of the present invention, which variations and modifications are within the scope of the present invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (37)
1. A method for preparing fuel by using high-acid-value biological grease comprises the following steps:
(a) carrying out thermal cracking deoxidation reaction on the high-acid-value biological grease under the heating condition;
(b) carrying out reduced pressure distillation on the product obtained in the step (a), and separating out water, a high-acid-value fraction, a low-acid-value fraction and heavy components;
(c) in the presence of a catalytic cracking deoxidation catalyst, carrying out catalytic cracking deoxidation reaction on the high-acid-value fraction obtained in the step (b) under the heating condition, and separating water and non-condensable gas;
(d) subjecting the mixture of the product obtained in step (c) and the low acid value fraction obtained in step (b) to catalytic hydrodeoxygenation with hydrogen in the presence of a hydrodeoxygenation catalyst under heating,
wherein the acid value of the high-acid value biological grease is more than or equal to 80mgKOH/g or the content of free fatty acid is more than or equal to 40 percent,
wherein the acid value of the high acid value fraction obtained in step (b) is in the range of 80 to 120mgKOH/g, and the acid value of the low acid value fraction is in the range of 10 to 50 mgKOH/g.
2. The process of claim 1, wherein steps (a), (b), and (d) are operated continuously, step (c) is operated continuously, or is operated intermittently.
3. The process of claim 2 wherein the batch operation of step (c) employs a multiple still cycle reaction.
4. The process of claim 2 wherein the continuous operation of step (c) employs a continuous catalytic distillation reaction.
5. The method of claim 1 wherein the high acid value biolipid is of animal origin, vegetable origin, microbial origin or mixtures of the foregoing.
6. The method of claim 1, wherein the heating conditions in step (a) are from 100 ℃ to 600 ℃.
7. The method of claim 1, wherein the high acid value biolipid in step (a) is thermally cracked and deoxygenated for 1 to 60 minutes.
8. The process of claim 1, wherein the product of step (a) comprises alkenes, alkanes, ketones, fatty acids, fatty alcohols, carbon monoxide, carbon dioxide, water.
9. The process of claim 1 wherein the product of step (b) comprises water, a high acid number fraction, a low acid number fraction, heavies, carbon dioxide, carbon monoxide.
10. The process of claim 1 wherein the heavies of step (b) are disposed of as waste or mixed with feed as feed to step (a).
11. The process of claim 1, wherein step (b) is carried out at a pressure of-0.05 MPa to-0.3 MPa.
12. The method of claim 1, wherein step (b) is performed at a temperature in the range of 100 ℃ to 500 ℃.
13. The process of claim 1 wherein the catalytic cracking deoxygenation catalyst of step (c) is selected from the group consisting of alumina, molecular sieves, silicon carbide, or mixtures thereof.
14. The process of claim 1, wherein step (C) is carried out at a temperature in the range of 100 ℃ to 500 ℃.
15. The process of claim 1, wherein step (d) is carried out at a temperature in the range of from 200 ℃ to 400 ℃, a hydrogen partial pressure in the range of from 1MPa to 6MPa, and a volume space velocity of 0.5h-1To 4.0h-1The volume ratio of hydrogen to oil is 200-1200: 1.
16. The method of claim 1, further comprising:
(e) fractionating the product of step (d) to obtain a gasoline component, a diesel component and a heavy component of >365 ℃.
17. The process of claim 16 wherein the high acid number fraction of step (b) is combined with a heavier than 365 ℃ as part of the feedstock for the catalytic cracking deoxygenation reaction.
18. The method of claim 1, wherein step (a) further comprises the step of preheating the high acid value biolipid.
19. The process of claim 1, wherein the hydrodeoxygenation catalyst is a supported metal catalyst or a metal sulfide.
20. The process of claim 4 wherein the fractions obtained from the continuous catalytic distillation are used as feed for the catalytic hydrodeoxygenation reaction in step (d).
21. The process of claim 1, wherein the product obtained in step (c) has an acid number of <50 mgKOH/g.
22. A system for producing fuel from high acid value biolipids comprising:
the thermal cracking reactor is used for receiving the high-acid-value biological grease and carrying out thermal cracking deoxidation reaction on the high-acid-value biological grease under the heating condition;
the reduced pressure distillation tower is connected with the thermal cracking reactor, receives a product obtained by thermal cracking deoxidation reaction, performs reduced pressure distillation, and separates out water, a high acid value fraction, a low acid value fraction, heavy components and non-condensable gas;
the catalytic cracking deoxidation reactor is connected with the reduced pressure distillation tower, and is used for carrying out catalytic cracking deoxidation reaction on the high-acid-value fraction obtained by reduced pressure distillation in the presence of a catalytic cracking deoxidation catalyst under the heating condition to separate water and non-condensable gas;
a hydrorefining reaction tower which receives and mixes the product from the catalytic cracking and deoxygenation reactor and the low acid value fraction from the vacuum distillation tower, and performs catalytic hydrodeoxygenation reaction with hydrogen under the heating condition in the presence of a hydrodeoxygenation catalyst,
wherein the acid value of the high-acid value biological grease is more than or equal to 80mgKOH/g or the content of free fatty acid is more than or equal to 40 percent,
wherein the acid value of the fraction with high acid value is in the range of 80-120mgKOH/g, and the acid value of the fraction with low acid value is in the range of 10-50 mgKOH/g.
23. The system of claim 22, wherein the catalytic cracking deoxygenation reactor employs a multi-still or catalytic distillation column.
24. The system of claim 22, wherein the high acid value biolipid is of animal origin, vegetable origin, microbial origin, or mixtures of the foregoing.
25. The system of claim 22 wherein the thermal cracking reactor is operated at 100 ℃ to 600 ℃ and the high acid value biological grease has a residence time in the thermal cracking reactor of 1 to 60 minutes.
26. The system of claim 22, wherein the products of the thermal cracking reactor comprise olefins, alkanes, ketones, fatty acids, fatty alcohols, carbon monoxide, carbon dioxide, water.
27. The system of claim 22, wherein the product of the vacuum distillation column comprises water, a high acid number fraction, a low acid number fraction, heavies, carbon dioxide, carbon monoxide.
28. The system of claim 22, wherein the heavy components from the vacuum distillation tower are disposed of as waste or mixed with feedstock as feedstock for a thermal cracking reactor.
29. The system of claim 22, wherein the pressure in the reduced pressure distillation column is from-0.05 MPa to-0.3 MPa and the temperature is from 200 ℃ to 500 ℃.
30. The system of claim 22, wherein the catalytic cracking deoxygenation catalyst is selected from the group consisting of alumina, molecular sieves, silicon carbide, or mixtures thereof.
31. The system of claim 22, wherein the heating conditions of the catalytic cracking deoxygenation reactor are between 100 ℃ and 500 ℃.
32. The system of claim 22, wherein the hydrodeoxygenation catalyst is a supported metal catalyst or a metal sulfide.
33. The system of claim 22, wherein the hydrofining reaction tower has a heating condition of 200 ℃ to 400 ℃, a hydrogen partial pressure of 1MPa to 6MPa, and a volume space velocity of 0.5h-1To 4.0h-1The volume ratio of hydrogen to oil is 200-1200: 1.
34. The system of claim 22 further comprising an atmospheric distillation column coupled to the hydrofinishing reaction column for fractionating the products of the hydrofinishing reaction column to yield a gasoline component, a diesel component and heavier components >365 ℃.
35. The system of claim 34 wherein heavier components >365 ℃ can be mixed with the high acid number fraction obtained from the vacuum distillation column as part of the feed to the catalytic cracking deoxygenation reactor.
36. The system of claim 22, wherein said system further comprises a preheater coupled to said thermal cracking reactor for preheating high acid value biolipids entering said thermal cracking reactor.
37. The system of claim 22, wherein the acid value of the product of the catalytic cracking deoxygenation reactor is <50 mgKOH/g.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910104447.6A CN109913256B (en) | 2019-02-01 | 2019-02-01 | Method and system for preparing fuel by using high-acid-value biological grease |
| EP20749511.0A EP3919588B1 (en) | 2019-02-01 | 2020-01-22 | Method and system for preparing fuel by using high acid value biological oil and fat |
| FIEP20749511.0T FI3919588T3 (en) | 2019-02-01 | 2020-01-22 | Method and system for preparing fuel by using high acid value biological oil and fat |
| PCT/CN2020/073766 WO2020156421A1 (en) | 2019-02-01 | 2020-01-22 | Method and system for preparing fuel by using high acid value biological oil and fat |
| US17/390,941 US12006484B2 (en) | 2019-02-01 | 2021-07-31 | Method and system for preparing fuel by using high acid value biological oil and fat |
| US18/656,265 US20240287398A1 (en) | 2019-02-01 | 2024-05-06 | Method and System for Preparing Fuel by Using High Acid Value Biological Oil and Fat |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102492455A (en) * | 2011-12-16 | 2012-06-13 | 易高环保能源研究院有限公司 | Method for preparing fuel from biological grease |
| CN102746871A (en) * | 2011-06-13 | 2012-10-24 | 易高环保能源研究院有限公司 | Method for preparing fuel from biological oil |
| CN103666520A (en) * | 2013-11-19 | 2014-03-26 | 张京三 | Method for producing hydrocarbon fuel oil by utilizing vegetable oil |
| CN108026450A (en) * | 2015-09-07 | 2018-05-11 | 国际壳牌研究有限公司 | Biomass is changed into liquid hydrocarbon materials |
| CN211570563U (en) * | 2019-02-01 | 2020-09-25 | 易高环保能源研究院有限公司 | System for preparing fuel by utilizing high-acid-value biological grease |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US8193399B2 (en) * | 2008-03-17 | 2012-06-05 | Uop Llc | Production of diesel fuel and aviation fuel from renewable feedstocks |
| US8039682B2 (en) * | 2008-03-17 | 2011-10-18 | Uop Llc | Production of aviation fuel from renewable feedstocks |
| US20090300971A1 (en) * | 2008-06-04 | 2009-12-10 | Ramin Abhari | Biorenewable naphtha |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746871A (en) * | 2011-06-13 | 2012-10-24 | 易高环保能源研究院有限公司 | Method for preparing fuel from biological oil |
| CN102492455A (en) * | 2011-12-16 | 2012-06-13 | 易高环保能源研究院有限公司 | Method for preparing fuel from biological grease |
| CN103666520A (en) * | 2013-11-19 | 2014-03-26 | 张京三 | Method for producing hydrocarbon fuel oil by utilizing vegetable oil |
| CN108026450A (en) * | 2015-09-07 | 2018-05-11 | 国际壳牌研究有限公司 | Biomass is changed into liquid hydrocarbon materials |
| CN211570563U (en) * | 2019-02-01 | 2020-09-25 | 易高环保能源研究院有限公司 | System for preparing fuel by utilizing high-acid-value biological grease |
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