A production method of aviation kerosene

Abstract

The present invention relates to the technical field of aviation kerosene production, and particularly to a production method of aviation kerosene, which includes: gasifying and converting low-carbon raw materials to generate conversion gas; obtaining crude syngas through a water washing and dust removal process for the conversion gas; subjecting the crude syngas to acid gas removal treatment through a purification device to obtain purified gas containing carbon monoxide, hydrogen, and carbon dioxide; using clean energy in an electrolyzer to obtain hydrogen and oxygen, storing and compressing the hydrogen separately, and sending the oxygen to a gasification device for gasification reaction; generating Fischer-Tropsch synthesis feed gas by passing the compressed hydrogen and the purified gas through a Fischer-Tropsch reaction device; and generating aviation fuel, gasoline, and diesel by passing the Fischer-Tropsch synthesis feed gas through a green aviation fuel synthesis reactor, a secondary flash evaporator, and a distillation column. By using low-carbon raw materials as raw materials for bio-aviation kerosene, the present invention can reduce the dependence on fossil fuels and increase the production of bio-aviation kerosene, thereby enabling large-scale promotion.

Description

Technical Field

[0001] The present invention relates to the technical field of aviation kerosene production, and particularly to a production method of aviation kerosene. Background Art

[0002] Green jet fuel, also known as biojet fuel, has the greatest advantage of reducing carbon dioxide emissions compared with traditional petroleum-based aviation kerosene. Common raw materials of green jet fuel mainly include various sustainable raw materials such as used cooking oil, agricultural and forestry waste, and algae.

[0003] Currently, bio-aviation kerosene is mainly produced from a variety of animal and vegetable oils and fats through a hydrogenation technology process under a certain catalyst system. However, limited by the insufficient supply at the raw material end, the current production capacity of biojet fuel is limited, and the production cost is also relatively high, which is not conducive to market promotion.

[0004] The global amount of agricultural and forestry waste is much larger than that of used cooking oil, and the production technology of converting biomass into aviation kerosene through gasification and Fischer-Tropsch synthesis has gradually matured, and the production cost has been continuously decreasing. The future prospect of producing biojet fuel from agricultural and forestry waste is also getting better and better.

[0005] Chinese Patent Publication No. CN111978984A discloses a method for producing aviation kerosene from aviation kerosene and coal tar, including the following steps: hydrofining reaction of coal tar, carrying out refining reactions such as hydrodesulfurization, hydrodenitrogenation, and aromatic saturation, and then contacting with a hydrocracking catalyst to carry out the branching reaction of alkanes and alkyl side chains.

[0006] In the prior art, since bio-aviation kerosene is mainly made from a variety of animal and vegetable oils and fats, the output is insufficient, the dependence on fossil fuels is relatively strong, and large-scale promotion cannot be carried out. Summary of the Invention

[0007] Therefore, the present invention provides a production method of aviation kerosene to overcome the problems in the prior art that due to the fact that bio-aviation kerosene is mainly made from a variety of animal and vegetable oils and fats, the output is insufficient, the dependence on fossil fuels is relatively strong, and large-scale promotion cannot be carried out.

[0008] To achieve the above object, the present invention provides a production method of aviation kerosene, including the following steps:

[0009] Feeding a low-carbon raw material into a gasification device to generate a gasification product gas, and partially oxidizing and non-catalytically reacting the gasification product gas through a conversion device to convert it into carbon monoxide and hydrogen;

[0010] Subjecting the converted carbon monoxide and hydrogen to a water washing and dust removal process to obtain a crude synthesis gas;

[0011] The crude syngas is subjected to acid gas removal and partial carbon dioxide treatment through a purification device to obtain purified gas containing carbon monoxide, hydrogen, and carbon dioxide;

[0012] Hydrogen and oxygen are obtained by using clean energy in an electrolyzer, and the hydrogen is stored and compressed respectively, and the oxygen and air are sent to the gasification device for gasification reaction;

[0013] The compressed hydrogen and the purified gas are used to generate Fischer-Tropsch synthesis feed gas through a Fischer-Tropsch reaction device;

[0014] The Fischer-Tropsch synthesis feed gas is used to generate aviation fuel, gasoline, and diesel through a green aviation fuel synthesis reactor, a secondary flash evaporator, and a distillation column;

[0015] The flow monitoring device monitors the conversion process of the conversion device by setting a periodic detection time, divides the periodic detection time into primary adjustment and secondary adjustment according to the crude syngas flow values in adjacent intervals, determines whether to start the primary adjustment according to the comparison result of the crude syngas flow within the detection time of adjacent intervals, generates a flow monitoring score according to the crude syngas flow after secondary adjustment, and determines whether to stop the conversion reaction according to the flow monitoring score.

[0016] Furthermore, the low-carbon raw material and the gasifying agent undergo a non-catalytic partial oxidation reaction in the gasification device to generate hydrogen, carbon monoxide, and carbon dioxide, and the reaction temperature range is 1000°C - 1500°C, and the reaction pressure range is 0.5 MPa - 6.5 MPa.

[0017] Furthermore, the gasification device operates using fixed-bed pressurized gasification technology, wherein the gasification technology operates above the ash fusion point; the fixed bed is successively a drying layer, a dry distillation layer, a gasification layer, and a combustion layer from top to bottom; the operating conditions of the fixed-bed pressurized technology are that the gasification temperature is 1100°C - 1500°C, and the gasification pressure is 0.5 MPa - 6.0 MPa.

[0018] Before entering the purification process, the crude syngas needs to be cooled to -15°C to -40°C. The hydrogen sulfide obtained after the purification of the crude syngas is used to produce sulfur through sulfur recovery, and carbon dioxide is liquefied to synthesize chemicals; the purification process uses the low-temperature methanol washing process or uses methyldiethanolamine for purification.

[0019] Furthermore, the Fischer-Tropsch synthesis feed gas is synthesized from the compressed hydrogen and the purified gas in a ratio of hydrogen to carbon molar ratio of 2.0 - 2.1, and the Fischer-Tropsch synthesis feed gas undergoes a synthesis reaction with a cobalt-based or iron-based catalyst in a green aviation fuel synthesis reactor to generate gaseous and liquid hydrocarbon substances.

[0020] Further, through the Fischer-Tropsch synthesis reaction, gaseous light hydrocarbons, olefins, synthetic oil, and synthetic wax are obtained. The synthetic oil and the synthetic wax are added into a hydroisomerization reactor for a chemical reaction. Among them, the hydroisomerization reactor contains a cracking catalyst and an isomerization catalyst for the reaction to obtain a hydroisomerization product. The hydroisomerization product is subjected to a hydro-saturation reaction to obtain green aviation fuel (C8-C16), gasoline (C5-C7), diesel (C17-C20), and naphtha or liquefied petroleum gas.

[0021] Compared with the prior art, the beneficial effects of the present invention are that it can continuously and stably utilize low-carbon raw materials to gasify and produce tar-free syngas, couple green electricity and green hydrogen to synthesize green aviation fuel, improve the production capacity of green aviation fuel, reduce the production cost of green aviation fuel, and stabilize the aviation fuel yield at more than 70%, effectively realizing the high-value recycling of low-carbon raw materials.

[0022] Further, the conversion process is monitored in segments according to the periodic detection time, which can better detect the conversion process to ensure the integrity of the conversion process. The flow monitoring device adjusts the periodic detection time multiple times, which can ensure that each conversion raw material in the conversion device is fully converted to improve the conversion efficiency, avoid wasting resources due to too long conversion time, and shorten the service life of the device.

[0023] Further, the flow monitoring device makes a primary adjustment to the periodic detection time according to the comparison result of the segmented raw syngas flow rates. If the raw syngas flow rate in the subsequent detection time is less than that in the previous detection time, the flow monitoring device makes a primary adjustment to the periodic detection time according to the comparison result of the segmented raw syngas flow rates, which can accurately reflect the reaction trend in the conversion process and more precisely understand the conversion reaction process in the conversion device.

[0024] Further, the flow monitoring device determines whether to make a secondary adjustment to the periodic monitoring time according to the comparison result of the slope within the interval during the periodically monitored time after the primary adjustment and the slope of the preset trigger condition for the secondary adjustment of the periodic monitoring time, which can effectively and more accurately estimate the conversion reaction in the subsequent stage of the conversion process.

[0025] Further, by orderly combining process routes such as gasifying the low-carbon raw materials to generate the raw syngas, converting the raw syngas, producing green hydrogen from green electricity, and synthesizing green aviation fuel, a qualified green aviation fuel product is finally obtained, and the carbon emissions in the production of green aviation fuel are effectively reduced through technological upgrading.

[0026] Furthermore, the conversion device efficiently achieves the conversion of methane in the gas from the gasifier outlet. At the same time, it directly cracks the multi-hydrocarbon substances and carbon-rich raw materials in tar into small molecule substances such as carbon monoxide, carbon dioxide, and hydrogen, so that there are no hydrocarbon, phenolic, and oil compounds in the subsequent syngas purification water, and there is no need for a large amount of water washing. This reduces the treatment volume of syngas washing wastewater, with low energy consumption, little pollution, and significantly reduced operating costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 is the operation flowchart of the production method of aviation kerosene in this embodiment;

[0028] Figure 2 is the process flowchart of synthesizing green aviation fuel from Fischer-Tropsch synthesis feed gas in the production method of aviation kerosene in this embodiment;

[0029] Figure 3 is the schematic flowchart of the production method of aviation kerosene in this embodiment;

[0030] Figure 4 is the process flowchart of the conversion process adjustment in the production method of aviation kerosene in this embodiment. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0031] In order to make the objectives and advantages of the present invention clearer, the present invention will be further described below in conjunction with embodiments; it should be understood that the specific embodiments described herein are only used to explain the present invention and are not used to limit the present invention.

[0032] The preferred embodiments of the present invention will be described below with reference to the accompanying drawings. Those skilled in the art should understand that these embodiments are only used to explain the technical principles of the present invention and do not limit the protection scope of the present invention.

[0033] It should be noted that in the description of the present invention, the terms indicating directions or positional relationships such as "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings. This is only for convenience of description and does not indicate or imply that the device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present invention.

[0034] In addition, it should also be noted that in the description of the present invention, unless otherwise clearly specified and limited, the terms "installation", "connection", and "connection" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two elements. For those skilled in the art, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0035] Please refer to Figures 1-4 as shown Figure 1 in the operation flowchart of the production method of aviation kerosene in this embodiment; Figure 2 in the process flowchart of the synthesis of green aviation fuel from the Fischer-Tropsch synthesis feed gas in the production method of aviation kerosene in this embodiment; Figure 3 in the schematic flowchart of the production method of aviation kerosene in this embodiment; Figure 4 in the process flowchart of the conversion process adjustment of the production method of aviation kerosene in this embodiment.

[0036] This embodiment provides a production method of aviation kerosene, including the following steps,

[0037] Step S100, feeding low-carbon raw materials into a gasification device to generate a gasified product gas, and the gasified product gas undergoes a partial oxidation non-catalytic reaction with oxygen through a conversion device to be converted into a conversion gas containing carbon monoxide, carbon dioxide, and hydrogen;

[0038] Step S200, obtaining a crude synthesis gas by subjecting the conversion gas to a water washing and dust removal process;

[0039] Step S300, a flow monitoring device is provided at the outlet of the conversion device, capable of measuring the flow rate of the crude synthesis gas;

[0040] Step S400, subjecting the crude synthesis gas to a treatment for removing acidic gases and part of carbon dioxide through a purification device to obtain a purified gas containing carbon monoxide, hydrogen, and carbon dioxide;

[0041] Step S500, obtaining hydrogen and oxygen by using clean energy for an electrolytic water device, storing and compressing the hydrogen respectively, and sending the oxygen and water vapor to the gasification device for a gasification reaction;

[0042] Step S600, generating a Fischer-Tropsch synthesis feed gas by mixing the compressed hydrogen and the purified gas through a Fischer-Tropsch reaction device;

[0043] Step S700, generating aviation fuel, gasoline, and diesel by passing the Fischer-Tropsch synthesis feed gas through a green aviation fuel synthesis reactor, a hydroisomerization reactor, a secondary flash evaporator, and a distillation tower.

[0044] Specifically, the flow monitoring device monitors the conversion process of the conversion device by setting a periodic detection time.

[0045] Specifically, the flow monitoring device divides the periodic detection time into a primary adjustment and a secondary adjustment according to the flow rate values of the crude synthesis gas in adjacent intervals.

[0046] Specifically, the flow monitoring device determines whether to initiate the primary adjustment according to the comparison result of the flow rate of the crude synthesis gas within the detection time in adjacent intervals.

[0047] Specifically, the flow rate monitoring device generates a flow rate monitoring score based on the flow rate of the roughly synthesized gas after secondary regulation, and determines whether to stop the reforming reaction according to the flow rate monitoring score.

[0048] Specifically, the flow rate monitoring device is provided with a periodic detection time T to monitor the flow rate of the roughly synthesized gas, and divides the reforming process time into a first interval detection time T1, a second interval detection time T2, a third interval detection time T3,..., an nth interval detection time Tn according to the periodic detection time T. Any ith interval detection time Ti is obtained, where i = 1, 2, 3,..., n, and the corresponding flow rate Ai of the roughly synthesized gas is obtained according to any ith interval detection time Ti.

[0049] If the flow rate Ai of the roughly synthesized gas detected by the flow rate monitoring device within the ith interval detection time Ti is less than the flow rate Ai+1 of the roughly synthesized gas within the (i + 1)th interval detection time Ti+1, the periodic monitoring time T does not need to be adjusted once.

[0050] If the flow rate Ai of the roughly synthesized gas detected within the ith interval detection time Ti is greater than or equal to the flow rate Ai+1 of the roughly synthesized gas within the (i + 1)th interval detection time Ti+1, the flow rate monitoring device adjusts the periodic monitoring time T once.

[0051] After one adjustment, the periodic monitoring time is Tia, and Tia = K × j, where K is the weight of the low-carbon raw material and j is the influence compensation parameter of the weight of the low-carbon raw material on the one-time adjustment of the periodic monitoring time.

[0052] The flow rate monitoring device is provided with a trigger condition for the secondary adjustment of the periodic monitoring time T, which is that the slope Bia of the flow rate interval of the roughly synthesized gas in any detection period after one adjustment is less than or equal to the standard slope B`.

[0053] Select the slope Bia of the flow rate interval of the roughly synthesized gas in any detection period after one adjustment. If Bia is less than or equal to the standard slope B`, the trigger condition for the secondary adjustment of the periodic monitoring time T set by the flow rate monitoring device is triggered, and the periodic monitoring time T is adjusted twice.

[0054] The period monitoring time after the secondary adjustment is Tib. At this time, the flow monitoring device generates a monitoring score F for the raw syngas flow value, where F = Bib×q1 + Bi+1b×q2 + (Bi+1b - Bib)×q3. Here, Bib is the slope of the interval within any period monitoring time Tib and Ti+1b after the secondary adjustment, q1 is the compensation parameter for the influence of the slope Bib of the interval within any period monitoring time Tib and Ti+1b after the secondary adjustment on the monitoring score of the raw syngas flow value; Bi+1b is the slope of the interval within the period monitoring time Ti+1b and Ti+2b after the secondary adjustment, q2 is the compensation parameter for the influence of the slope Bi+1b of the interval within any period monitoring time Ti+1b and Ti+2b after the secondary adjustment on the monitoring score of the raw syngas flow value, Bi+1b - Bib is the difference in the slope of the interval between Bi+1b and Bib after the secondary adjustment, and q3 is the compensation parameter for the influence of the difference in the slope of the interval between Bi+1b and Bib after the secondary adjustment on the monitoring score of the raw syngas flow value;

[0055] The flow monitoring device preset a first monitoring score F1 for the raw syngas flow value.

[0056] If F ≤ F1, the conversion device stops the conversion.

[0057] In this embodiment, the raw syngas flow A5 corresponding to the fifth detection time T5 and the raw syngas flow A6 corresponding to the sixth detection time T6 are selected.

[0058] If A5 < A6, the period monitoring time T does not need to be adjusted.

[0059] If A5 ≥ A6, the flow monitoring device makes a primary adjustment to the period monitoring time T.

[0060] The period monitoring time after the primary adjustment is Tia. The period monitoring times T4a and T5a after the primary adjustment are selected, and the slope of the raw syngas flow interval is B4a.

[0061] If B4a ≤ B`, the flow monitoring device makes a secondary adjustment to the period monitoring time T.

[0062] The post-secondary regulation cycle monitoring time is Tib. The flow monitoring device generates a monitoring score F for the raw syngas flow value, where F = B2b×q1 + B3b×q2 + (B3b - B2b)×q3. Here, B2b is the slope within the interval between the post-secondary regulation cycle monitoring times T2b and T3b, q1 is the compensation parameter for the influence of the slope B2b within the interval between the post-secondary regulation cycle monitoring times T2b and T3b on the monitoring score of the raw syngas flow value; B3b is the slope within the interval between the post-secondary regulation cycle monitoring times T3b and T4b, q2 is the compensation parameter for the influence of the slope B3b within the interval between the post-secondary regulation cycle monitoring times T3b and T4b on the monitoring score of the raw syngas flow value, B3b - B2b is the difference in the slopes between B3b and B2b after secondary regulation, and q3 is the compensation parameter for the influence of the difference in the slopes between B3b and B2b after secondary regulation on the monitoring score of the raw syngas flow value;

[0063] The flow monitoring device presets a first monitoring score F1 for the raw syngas flow value.

[0064] If F ≤ F1, the conversion device stops conversion.

[0065] The beneficial effects of the present invention are that it can continuously and stably use low-carbon raw materials for gasification to produce tar-free syngas, couple green electricity and green hydrogen to synthesize green aviation fuel, improve the production capacity of green aviation fuel, reduce the production cost of green aviation fuel, and stabilize the aviation fuel yield at about 70%, effectively realizing the high-value recycling of low-carbon raw materials.

[0066] Specifically, by segmenting and monitoring the conversion process according to the periodic detection time, the conversion process can be better detected to ensure the integrity of the conversion process. The flow monitoring device adjusts the periodic detection time multiple times, which can ensure that each conversion raw material in the conversion device is fully converted to improve the conversion efficiency, avoid wasting resources due to too long conversion time, and shorten the service life of the device.

[0067] Specifically, the flow monitoring device makes a primary adjustment to the periodic detection time according to the comparison result of the segmented raw syngas flow. If the raw syngas flow in the subsequent detection time is less than that in the previous detection time, the flow monitoring device makes a primary adjustment to the periodic detection time according to the comparison result of the segmented raw syngas flow, which can accurately reflect the reaction trend in the conversion process and more precisely understand the conversion reaction process in the conversion device.

[0068] Specifically, the flow monitoring device determines whether to make a secondary adjustment to the periodic monitoring time according to the comparison result between the slope within the interval of the periodic monitoring time after the primary adjustment and the slope of the preset trigger condition for the secondary adjustment of the periodic monitoring time, which can effectively and more accurately estimate the conversion reaction in the subsequent stage of the conversion process.

[0069] Specifically, the low-carbon raw materials and the gasifying agent undergo a non-catalytic partial oxidation reaction in the gasification device, generating hydrogen, carbon monoxide, and carbon dioxide. The reaction temperature range is 1000°C - 1500°C, and the reaction pressure range is 0.5 MPa - 6.5 MPa.

[0070] Specifically, the gasification device operates using the fixed-bed pressurized gasification technology. In the fixed-bed pressurized gasification technology, the fixed bed, from top to bottom, is successively the drying layer, the dry distillation layer, the gasification layer, and the combustion layer. The operating conditions of the fixed-bed pressurized technology are that the gasification temperature is 1000°C - 1500°C, and the gasification pressure is 0.5 MPa - 6.0 MPa.

[0071] Specifically, the conversion device efficiently realizes the conversion of methane in the gasified furnace outlet gas, and at the same time, the rich-carbon raw materials in polyhydrocarbons and tar are cracked into small-molecule substances such as carbon monoxide, carbon dioxide, and hydrogen in one step, so that there are no hydrocarbon, phenol, and oil compounds in the subsequent syngas purification water, and there is no need for a large amount of water washing. This makes the treatment volume of the syngas washing wastewater small, with low energy consumption, little pollution, and significantly reduced operating costs.

[0072] Specifically, before entering the purification process, the raw syngas needs to be cooled to -15°C to -40°C. The hydrogen sulfide obtained after the purification of the raw syngas is used to produce sulfur by sulfur recovery, and carbon dioxide is liquefied to synthesize chemicals. The purification process uses the low-temperature methanol washing process or uses methyldiethanolamine for purification.

[0073] Specifically, the Fischer-Tropsch synthesis feed gas is synthesized from the compressed hydrogen and the purified gas at a hydrogen-carbon molar ratio of 2.0 - 2.1. The Fischer-Tropsch synthesis feed gas undergoes a synthesis reaction with a cobalt-based or iron-based catalyst in the green aviation fuel synthesis reactor to generate gaseous and liquid hydrocarbon substances.

[0074] Specifically, through the Fischer-Tropsch synthesis reaction, gaseous low-carbon hydrocarbons, olefins, synthetic oil, and synthetic wax are obtained. The synthetic oil and the synthetic wax are added to the hydroisomerization reactor for a chemical reaction. Among them, the hydroisomerization reactor contains cracking catalyst and isomerization catalyst for the reaction to obtain hydroisomerization products, and the hydroisomerization products are subjected to a hydrogenation saturation reaction to obtain green aviation fuel (C8 - C16), gasoline (C5 - C7), diesel (C17 - C20), and naphtha or liquefied petroleum gas.

[0075] This embodiment provides a process for synthesizing green aviation fuel from the Fischer-Tropsch synthesis feed gas in a production method of aviation kerosene, including,

[0076] Step S611: Mix the purified gas generated in the purification process with the hydrogen gas generated in the electrolytic water hydrogen production process to form a Fischer-Tropsch synthesis feed gas with a hydrogen-carbon molar ratio of 2.0 - 2.1. Feed the feed gas into a green jet fuel synthesis reactor and carry out a synthesis reaction under the action of a cobalt-based or iron-based catalyst to generate gaseous and liquid hydrocarbon substances;

[0077] Step S612: After the Fischer-Tropsch synthesis product is cooled, it enters a secondary flash separator to separate out gaseous, oil-phase, and wax-phase products;

[0078] Step S613: The gaseous product is separated by pressure swing adsorption to obtain the hydrogen required for the hydrocracking reaction; the wax-phase product enters a hydrocracking reactor to crack the high-carbon-number wax phase into low-carbon-chain alkanes, and the cracking products are separated by secondary flashing to obtain three-phase products;

[0079] Step S614: Mix the hydrocracking oil-phase product with the Fischer-Tropsch oil-phase product and carry out rectification separation through a distillation column to obtain green jet fuel (C8 - C16), gasoline (C5 - C7), diesel (C17 - C20), and naphtha or liquefied petroleum gas.

[0080] Specifically, by orderly combining processes such as gasifying the low-carbon raw material to generate the crude syngas, converting the crude syngas, producing green hydrogen by green electricity, and synthesizing green jet fuel, a qualified green jet fuel product is finally obtained, and the carbon emissions in green jet fuel production are effectively reduced through technological upgrading.

[0081] Example 1 uses corn straw as a low-carbon raw material for the production of aviation kerosene. The specific steps of the production method include,

[0082] Step 1: Prepare corn straw into cylinders with a particle size of 8 - 10 mm and a length of 10 - 30 mm. Add the particles into the gasification device through a feeding device and carry out gasification under the operating conditions of a steam-to-oxygen flow ratio of 0.7:0.9, a gasification pressure of 4.0 MPa, and a gasification temperature of 1150 °C. Feed the gasification product gas into the conversion device;

[0083] The gasification product gas of the gasification device undergoes a non-catalytic partial oxidation reaction with oxygen in the conversion device. The conversion operation temperature is 1050 °C, and more than 99.9% of methane, oil, and polyhydrocarbons in the gasification product gas are converted into hydrogen, carbon monoxide, and carbon dioxide. The gas at the outlet of the conversion device enters the dust collector;

[0084] Through water washing and dust removal, the dust content in the gas at the outlet of the dust collector is reduced to less than 5 mg / m3, and the generated heat is recovered through a double-layer jacket to produce saturated steam with a production pressure of 2.8 MPa.

[0085] Step 2: The raw syngas is purified by low-temperature methanol washing. After purification, the content of H2S in the syngas is less than 0.03 mg / m3, and it does not contain impurities such as Cl-, Br-, Pb, Sn, and Bi. The purified H2S is used for sulfur recovery to produce sulfur.

[0086] Step 3: The purified gas produced after the purification process is mixed with the hydrogen produced through the electrolytic water hydrogen production process to form a Fischer-Tropsch synthesis feed gas with a hydrogen-carbon molar ratio of 2.05. The Fischer-Tropsch synthesis feed gas is introduced into a green aviation fuel synthesis reactor and undergoes a synthesis reaction under the action of a cobalt-based catalyst to generate gaseous and liquid hydrocarbon substances.

[0087] Step 4: Through the Fischer-Tropsch synthesis reaction, gaseous light hydrocarbons, olefins, synthetic oil, and synthetic wax are obtained. The synthetic oil and the synthetic wax are added to a hydroisomerization reactor for a chemical reaction. Among them, the hydroisomerization reactor contains cracking catalysts and isomerization catalysts for the reaction to obtain hydroisomerization products. The hydroisomerization products are subjected to a hydro-saturation reaction, and the products of the hydro-saturation reaction are separated by rectification through a distillation column to obtain green aviation fuel (C8-C16), gasoline (C5-C7), diesel (C17-C20), and naphtha or liquefied petroleum gas.

[0088] In Example 2, wheat straw is used as a low-carbon raw material for the production of aviation kerosene. The specific steps of the production method include:

[0089] Step 1: Wheat straw is prepared into particles with a particle size of 20-40 mm. The particles are added to a gasification device through a feeding device and gasified under the operating conditions of a steam-to-oxygen flow ratio of 0.85:1, a gasification pressure of 5.0 MPa, and a gasification temperature of 1250 °C. The gasified gas is sent into a conversion device.

[0090] The gasified gas from the gasification device undergoes a non-catalytic partial oxidation reaction with oxygen in the conversion device. The conversion operation temperature is 1100 °C. More than 99.9% of methane, oil, and polyhydrocarbons in the gasified gas are converted into hydrogen, carbon monoxide, and carbon dioxide. The gas at the outlet of the conversion device enters a dust collector.

[0091] Through water washing and dust removal, the dust content in the gas at the outlet of the dust collector reaches less than 4 mg / m3, and the generated heat is recovered through a double-layer jacket to produce saturated steam with a production pressure of 2.8 MPa.

[0092] Step 2: The raw syngas is purified by low-temperature methanol washing. After purification, the content of H2S in the syngas is less than 0.03 mg / m3, and it does not contain impurities such as Cl-, Br-, Pb, Sn, and Bi. The purified H2S is used for sulfur recovery to produce sulfur.

[0093] Step 3: Mix the purified gas generated after the purification process with the hydrogen generated in the electrolytic water hydrogen production process to form a Fischer-Tropsch synthesis feed gas with a hydrogen-carbon molar ratio of 2.1. Feed the Fischer-Tropsch synthesis feed gas into a green jet fuel synthesis reactor, and carry out a synthesis reaction under the action of a cobalt-based catalyst to generate gaseous and liquid hydrocarbon substances.

[0094] Step 4: Obtain gaseous light hydrocarbons, olefins, synthetic oil, and synthetic wax through the Fischer-Tropsch synthesis reaction. Add the synthetic oil and the synthetic wax into a hydroisomerization reactor for a chemical reaction. Among them, the hydroisomerization reactor contains a cracking catalyst and an isomerization catalyst for the reaction to obtain a hydroisomerization product. Carry out a hydrogenation saturation reaction on the hydroisomerization product, and separate the product of the hydrogenation saturation reaction through a distillation column to obtain green jet fuel (C8-C16), gasoline (C5-C7), diesel (C17-C20), and naphtha or liquefied petroleum gas.

[0095] In Example 3, miscanthus is used as a low-carbon raw material for the production of aviation kerosene. The specific steps of the production method include

[0096] Step 1: Prepare miscanthus into particles with a particle size of 20 mm - 40 mm. Add the particles into a gasification device through a feeding device, and carry out gasification under the operating conditions of a steam-to-oxygen flow ratio of 0.7:1.1, a gasification pressure of 5.4 MPa, and a gasification temperature of 1300 °C. The gas generated by the gasification of the gasification device undergoes a non-catalytic partial oxidation reaction with oxygen in a conversion device. The conversion operation temperature is 1280 °C. More than 99.9% of methane, oil, and polyhydrocarbons in the gas generated by gasification are converted into hydrogen, carbon monoxide, and carbon dioxide. The gas at the outlet of the conversion device enters a dust collector.

[0097] Through water washing and dust removal, the dust content in the gas at the outlet of the dust collector is reduced to less than 5 mg / m3. The heat generated is recovered through a double-layer jacket to produce saturated steam with a production pressure of 3.0 MPa.

[0098] Step 2: Purify the raw syngas through cold methanol washing. The content of H2S in the purified syngas is less than 0.03 mg / m3, and it does not contain impurities such as Cl-, Br-, Pb, Sn, and Bi. The purified H2S is used for sulfur recovery to produce sulfur.

[0099] Step 3: Mix the purified gas generated after the purification process with the hydrogen generated in the electrolytic water hydrogen production process to form a Fischer-Tropsch synthesis feed gas with a hydrogen-carbon molar ratio of 2.0. Feed the Fischer-Tropsch synthesis feed gas into a green jet fuel synthesis reactor, and carry out a synthesis reaction under the action of a cobalt-based catalyst to generate gaseous and liquid hydrocarbon substances;

[0100] Step 4: Obtain gaseous low-carbon hydrocarbons, olefins, synthetic oil, and synthetic wax through Fischer-Tropsch synthesis. Add the synthetic oil and the synthetic wax into a hydroisomerization reactor for chemical reaction. Among them, the hydroisomerization reactor contains cracking catalyst and isomerization catalyst for reaction to obtain a hydroisomerization product. Conduct a hydro-saturation reaction on the hydroisomerization product, and separate the product of the hydro-saturation reaction through rectification in a distillation column to obtain green aviation fuel (C8-C16), gasoline (C5-C7), diesel (C17-C20), and naphtha or liquefied petroleum gas.

[0101] So far, the technical solution of the present invention has been described in conjunction with the preferred embodiments shown in the drawings. However, it is easy for those skilled in the art to understand that the protection scope of the present invention is obviously not limited to these specific embodiments. Without departing from the principle of the present invention, those skilled in the art can make equivalent changes or substitutions to the relevant technical features, and the technical solutions after these changes or substitutions will all fall within the protection scope of the present invention.

[0102] The above are only the preferred embodiments of the present invention and are not used to limit the present invention; for those skilled in the art, the present invention can have various changes and modifications. Any modification, equivalent substitution, improvement, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. A method for producing aviation kerosene, characterized in that: The following steps are included: The low-carbon raw material is fed into a gasification device to generate a gasification product gas, and the gasification product gas is converted into a conversion gas containing carbon monoxide, carbon dioxide and hydrogen by a partial oxidation non-catalytic reaction with oxygen through a conversion device; The conversion gas is subjected to a water washing and dust removal process to obtain a crude synthesis gas; The gas outlet of the conversion device is provided with a flow monitoring device, which can measure the flow rate of the crude synthesis gas; The crude synthesis gas is passed through a purification device to remove acidic gas and part of carbon dioxide to obtain a purified gas containing carbon monoxide, hydrogen and carbon dioxide; By using clean energy in a water electrolysis device to obtain hydrogen and oxygen, the hydrogen is stored and compressed, and the oxygen and water vapor are sent to the gasification device for gasification reaction; Passing the compressed hydrogen and the purified gas through a Fischer-Tropsch reaction device to generate a Fischer-Tropsch synthesis feed gas; The Fischer-Tropsch synthesis feed gas is passed through a green aviation fuel synthesis reactor, a hydroisomerization reactor, a secondary flash evaporator and a distillation tower to generate aviation fuel, gasoline and diesel; The flow monitoring device monitors the conversion process of the conversion device by setting a periodic detection time, and divides the periodic detection time into primary adjustment and secondary adjustment according to the crude synthesis gas flow value in adjacent intervals. Whether to start the primary adjustment is determined based on the comparison result of the crude synthesis gas flow within the adjacent interval detection time, and a flow monitoring score is generated based on the crude synthesis gas flow after the secondary adjustment, and whether to stop the conversion reaction is determined based on the flow monitoring score.

2. The method for producing aviation kerosene according to claim 1, characterized in that: The low-carbon raw material and the gasifying agent undergo a non-catalytic partial oxidation reaction in the gasification device to generate hydrogen, carbon monoxide and carbon dioxide. The reaction temperature range is 1000° C.-1500° C., and the reaction pressure range is 0.5 MPa-6.5 MPa.

3. The method for producing aviation kerosene according to claim 2, characterized in that: The gasification device is operated by fixed bed pressurized gasification technology, and the fixed bed is composed of a drying layer, a distillation layer, a gasification layer and a combustion layer from top to bottom; the operating conditions of the fixed bed pressurized technology are a gasification temperature of 1100°C-1500°C and a gasification pressure of 0.5 MPa-6.0 MPa.

4. The method for producing aviation kerosene according to claim 3, characterized in that: The crude synthesis gas needs to be cooled to -15°C to -40°C before entering the purification process. The hydrogen sulfide obtained after the crude synthesis gas is purified is recovered by sulfur to produce sulfur, and carbon dioxide is liquefied to synthesize chemicals. The purification process adopts a low-temperature methanol washing process or uses methyldiethanolamine for purification.

5. The method for producing aviation kerosene according to claim 4, characterized in that: The Fischer-Tropsch synthesis feed gas is synthesized from the compressed hydrogen and the purified gas at a hydrogen-to-carbon molar ratio of 2.0-2.

1. The Fischer-Tropsch synthesis feed gas undergoes a synthesis reaction with a cobalt-based or iron-based catalyst in a green aviation fuel synthesis reactor to generate gaseous and liquid hydrocarbon substances.

6. The method for producing aviation kerosene according to claim 5, characterized in that: Olefins, synthetic oil and synthetic wax are obtained through Fischer-Tropsch synthesis reaction, and the synthetic oil and synthetic wax are added into a hydroisomerization reactor for chemical reaction, wherein the hydroisomerization reactor contains a cracking catalyst and an isomerization catalyst to obtain a hydroisomerization product, a hydrogenation saturation reaction is performed on the hydroisomerization product, and the product of the hydrogenation saturation reaction is separated by distillation through a distillation tower to obtain green aviation fuel, gasoline, diesel and naphtha or liquefied petroleum gas.

Images