CN116554928B - LPG air mixing preparation process for replacing natural gas - Google Patents
LPG air mixing preparation process for replacing natural gas Download PDFInfo
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- CN116554928B CN116554928B CN202310525812.7A CN202310525812A CN116554928B CN 116554928 B CN116554928 B CN 116554928B CN 202310525812 A CN202310525812 A CN 202310525812A CN 116554928 B CN116554928 B CN 116554928B
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- 238000002156 mixing Methods 0.000 title claims abstract description 115
- 239000003915 liquefied petroleum gas Substances 0.000 title claims abstract description 99
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 238000002360 preparation method Methods 0.000 title claims abstract description 24
- 239000003345 natural gas Substances 0.000 title claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 107
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 58
- 238000006243 chemical reaction Methods 0.000 claims abstract description 42
- 239000001273 butane Substances 0.000 claims abstract description 29
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 29
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000001294 propane Substances 0.000 claims abstract description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 24
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 24
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 22
- 238000002309 gasification Methods 0.000 claims abstract description 12
- 239000003570 air Substances 0.000 claims description 23
- 238000010438 heat treatment Methods 0.000 claims description 20
- 238000001816 cooling Methods 0.000 claims description 16
- 238000003795 desorption Methods 0.000 claims description 8
- 238000001035 drying Methods 0.000 claims description 8
- 238000001914 filtration Methods 0.000 claims description 8
- 238000011282 treatment Methods 0.000 claims description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 3
- 230000005284 excitation Effects 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 11
- 238000000034 method Methods 0.000 abstract description 9
- 230000008569 process Effects 0.000 abstract description 8
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 230000001105 regulatory effect Effects 0.000 description 16
- 239000000203 mixture Substances 0.000 description 14
- 230000006872 improvement Effects 0.000 description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/02—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the field of LPG mixing and air preparing, in particular to an LPG mixing and air preparing process for replacing natural gas. It comprises the following steps: s1, preparing mixed gas (A, B); s2, pressurizing the mixed gas (A, B); s3, introducing the prefabricated gas and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction; s4, further mixing the gas after hydrogenation reaction with the prefabricated LPG to form LPG empty mixing; the invention adopts low temperature plasma technology to carry out hydrogen reaction on propane and butane, improves the conversion rate of propane and butane, effectively reduces the energy cost, improves the yield and quality of LPG mixing space, and simultaneously can avoid the environmental pollution problem generated by the traditional LPG mixing space preparation technology.
Description
Technical Field
The invention relates to the field of LPG mixing and air preparing, in particular to an LPG mixing and air preparing process for replacing natural gas.
Background
LPG mixing is a novel fuel gas preparation technology, is formed by mixing LPG and air, and aims to replace the traditional natural gas. The combustion heat value of the gas-liquid mixed diesel fuel can be consistent with that of natural gas, and meanwhile, the gas mixing of LPG also has the advantage of rich resources, so that the gas-liquid mixed diesel fuel becomes an important alternative energy source.
At present, in the process of preparing the LPG mixing space, a key technology is how to realize the mixing of the LPG and the air in a strict proportion range, and the mixing flow cannot be reversed to avoid the risk of safe operation. Previously, people usually mix LPG, air and oxygen, but because oxygen can be prepared by special equipment, the technology is more complex and expensive, and the flow of LPG and air/oxygen is adjusted and mixed to generate LPG empty; however, a significant disadvantage of this mixing method is the generation of large amounts of nitrogen oxides, which are harmful to the environment and to human health. Moreover, the preparation of oxygen requires the preparation of ozone first, then the ozone is decomposed into oxygen by using an ozone producer, and the whole preparation process is complicated in technology and equipment; in view of this, there is an urgent need for a new LPG mix air preparation process for replacing natural gas to improve the shortcomings of the prior art.
Disclosure of Invention
The invention aims to provide an LPG mixing space preparation process for replacing natural gas, so as to solve the problems in the background art.
In order to achieve the above object, the present invention provides an LPG empty mixing preparation process for replacing natural gas, comprising the steps of:
s1, mixing propane and butane according to a proportion to form a mixed gas A; mixing propane, butane and air in proportion to form mixed gas B for preparing LPG prefabricated mixed air;
s2, pressurizing the mixed gas A, then respectively entering a mixing tower for mixing, heating the mixed gas by using an energy-saving heater, and then cooling to obtain gas to be hydrogenated; pressurizing the mixed gas B, then respectively entering a mixing tower for mixing, heating the mixed gas by a heater, and then cooling to obtain the prefabricated LPG;
s3, introducing the prefabricated gas and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction, and after the mixed gas enters the low-temperature plasma reactor, breaking chemical bonds in molecules through the excitation of plasma to generate methane and ethane through hydrogenation reaction;
and S4, further mixing the gas after the hydrogenation reaction with the prefabricated LPG to ensure that the mixing volume of the gas after the hydrogenation reaction is the same as the volume of the prefabricated LPG, thereby forming the LPG mixing space.
As a further improvement of the technical scheme, in the S1, the mixing volume ratio of propane to butane in the mixed gas A is 6-7:4-3.
As a further improvement of the technical scheme, in the S1, the mixing volume ratio of (propane and butane) and air in the mixed gas B is 5-6:5-4.
As a further improvement of the technical scheme, in the step S2, the heating temperature of the mixed gas A is 25-45 ℃.
As a further improvement of the technical scheme, in the step S2, the heating temperature of the mixed gas of the step B is 35-45 ℃.
As a further improvement of the technical scheme, in the step S2, the mixing equipment mainly comprises a mixer, and is provided with a mixing fan blade system and a filler layer.
As a further improvement of the present invention, in S2, the heater is preferably an energy-saving heater.
As a further improvement of the present technical solution, in S2, the pressurizing treatment adopts a multi-stage pressurizing manner.
As a further improvement of the technical scheme, in the S3, the hydrogenation reaction temperature is 60-80 ℃, the reaction pressure is 0.1-0.2Mpa, and the duration is 1-2h.
As a further improvement of the technical scheme, in S4, after the LPG mix space is formed, the LPG mix space is sent to a desorption tower, and the desired LPG mix space can be obtained through drying, filtering and other treatments.
Compared with the prior art, the invention has the beneficial effects that:
the low-temperature plasma technology is adopted to carry out the hydrogen gasification reaction on propane and butane, the conversion rate of the propane and the butane is improved, the energy cost is effectively reduced, the output and the quality of the LPG mixing space are improved, the environmental pollution problem caused by the traditional LPG mixing space preparation technology can be avoided, the process has the advantages of simplicity, environmental protection, practicability and the like, the process can be applied to LPG mixing space production of various scales, the low-temperature plasma technology is adopted to carry out the hydrogen gasification reaction, the reaction process is very stable, side reaction or excessive reaction is not easy to generate, and the obtained product has high purity and high yield.
Drawings
Fig. 1 is an overall flow diagram of the present invention.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
According to fig. 1, an embodiment of the present invention provides an LPG mix air preparation process for replacing natural gas, comprising the steps of:
firstly, mixing propane and butane according to a proportion to form a mixed gas A so as to carry out a subsequent hydrogen gasification reaction, and controlling the mixing proportion by adjusting the flow of the propane and the butane; mixing propane, butane and air in proportion to form mixed gas B for preparing LPG prefabricated mixed air;
wherein, the mixing volume ratio of propane to butane in the mixed gas A is 6-7:4-3; the mixing volume ratio of the (propane and butane) and the air in the mixed gas B is 5-6:5-4;
step two, pressurizing the mixed gas A, then respectively entering a mixing tower for mixing, heating the mixed gas to 25-45 ℃ by using a heater, and then cooling to obtain the gas to be hydrogenated; pressurizing the mixed gas B, then respectively mixing the mixed gas B in a mixing tower, heating the mixed gas to 35-45 ℃ by using a heater, and then cooling to obtain prefabricated LPG; the mixing tower takes a mixer as a main part and is provided with a mixing fan blade system and a filler layer; the heater is preferably an energy-saving heater, so that energy consumption can be reduced; the pressurizing treatment adopts a multi-stage pressurizing mode, so that the mixing effect can be effectively improved;
introducing the prefabricated gas and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction, and after the mixed gas enters the low-temperature plasma reactor, breaking chemical bonds in molecules through the excitation of plasma to further carry out a hydrogenation reaction to generate methane and ethane; the reaction temperature is regulated to be 60-80 ℃, the reaction pressure is regulated to be 0.1-0.2Mpa, the duration is regulated to be 1-2h, the products with high conversion rate and high yield can be obtained, and meanwhile, the occurrence of excessive reaction and side reaction can be avoided;
step four, the gas after hydrogenation reaction is further mixed with the prefabricated LPG, so that the mixing volume of the gas after hydrogenation reaction is the same as the volume of the prefabricated LPG, and LPG mixing space is formed; the LPG mixture is sent to a desorption tower, and the required LPG mixture can be obtained through drying, filtering and other treatments, and the purpose is to remove impurities and moisture in the mixed gas, so that the cleaner and purer LPG mixture is obtained.
The novel LPG mixing preparation process provided by the invention adopts the low-temperature plasma technology to carry out the hydrogen reaction on propane and butane, improves the conversion rate of the propane and the butane, effectively reduces the energy cost, improves the yield and the quality of LPG mixing, can avoid the environmental pollution problem generated by the traditional LPG mixing preparation process, has the advantages of simplicity, environmental protection, practicability and the like, can be applied to the LPG mixing production of various scales, adopts the low-temperature plasma technology to carry out the hydrogen reaction, has very stable reaction process, is not easy to produce side reaction or excessive reaction, and has high purity and high yield of the obtained product.
The LPG mix-air preparation process for replacing natural gas provided by the present invention is further described by the following specific examples according to the mixture ratio and process parameters of different mixed gases (a, B).
Example 1
Step one, mixing propane and butane according to a ratio of 7:3 to form mixed gas A; mixing propane, butane and air according to a ratio of 4.5:5.5 to form a mixed gas B;
step two, pressurizing the mixed gas A, then respectively entering a mixing tower for mixing, heating the mixed gas to 25 ℃ by using a heater, and then cooling to obtain gas to be hydrogenated; pressurizing the mixed gas B, then respectively mixing the mixed gas B with a mixing tower, heating the mixed gas to 35 ℃ by using a heater, and then cooling to obtain the prefabricated LPG;
introducing the prefabricated gas and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction; the reaction temperature is regulated to 40 ℃, the reaction pressure is regulated to 0.1Mpa, and the duration is regulated to 2 hours;
step four, the gas after hydrogenation reaction is further mixed with the prefabricated LPG, so that the mixing volume of the gas after hydrogenation reaction is the same as the volume of the prefabricated LPG, and LPG mixing space is formed; and (3) conveying the LPG mixed space to a desorption tower, and drying, filtering and the like to obtain the required LPG mixed space.
Example 2
Step one, mixing propane and butane according to a ratio of 6.5:3.5 to form mixed gas A; (propane, butane) and air in ratio 5:5, mixing to form a mixed gas B;
step two, pressurizing the mixed gas A, then respectively entering a mixing tower for mixing, heating the mixed gas to 45 ℃ by using a heater, and then cooling to obtain gas to be hydrogenated; pressurizing the mixed gas B, then respectively mixing the mixed gas B with a mixing tower, heating the mixed gas to 45 ℃ by using a heater, and then cooling to obtain the prefabricated LPG;
introducing the prefabricated gas and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction; the reaction temperature is regulated to 80 ℃, the reaction pressure is regulated to 0.2Mpa, and the duration is 1h;
step four, the gas after hydrogenation reaction is further mixed with the prefabricated LPG, so that the mixing volume of the gas after hydrogenation reaction is the same as the volume of the prefabricated LPG, and LPG mixing space is formed; and (3) conveying the LPG mixed space to a desorption tower, and drying, filtering and the like to obtain the required LPG mixed space.
Example 3
Step one, mixing propane and butane according to a ratio of 6:4 to form mixed gas A; mixing (propane and butane) with air according to a ratio of 5.5:4.5 to form a mixed gas B;
step two, pressurizing the mixed gas A, then respectively entering a mixing tower for mixing, heating the mixed gas to 40 ℃ by using a heater, and then cooling to obtain gas to be hydrogenated; pressurizing the mixed gas B, then respectively mixing the mixed gas B with a mixing tower, heating the mixed gas to 40 ℃ by using a heater, and then cooling to obtain the prefabricated LPG;
introducing the prefabricated gas and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction; the reaction temperature is regulated to 70 ℃, the reaction pressure is regulated to 0.15Mpa, and the duration time is regulated to 2 hours;
step four, the gas after hydrogenation reaction is further mixed with the prefabricated LPG, so that the mixing volume of the gas after hydrogenation reaction is the same as the volume of the prefabricated LPG, and LPG mixing space is formed; and (3) conveying the LPG mixed space to a desorption tower, and drying, filtering and the like to obtain the required LPG mixed space.
Example 4
Step one, mixing propane and butane according to a ratio of 5.5:4.5 to form mixed gas A; mixing (propane and butane) with air according to a ratio of 6:4 to form a mixed gas B;
step two, pressurizing the mixed gas A, then respectively entering a mixing tower for mixing, heating the mixed gas to 40 ℃ by using a heater, and then cooling to obtain gas to be hydrogenated; pressurizing the mixed gas B, then respectively mixing the mixed gas B with a mixing tower, heating the mixed gas to 45 ℃ by using a heater, and then cooling to obtain the prefabricated LPG;
introducing the prefabricated gas and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction; the reaction temperature is regulated to 80 ℃, the reaction pressure is regulated to 0.1Mpa, and the duration is 1h;
step four, the gas after hydrogenation reaction is further mixed with the prefabricated LPG, so that the mixing volume of the gas after hydrogenation reaction is the same as the volume of the prefabricated LPG, and LPG mixing space is formed; and (3) conveying the LPG mixed space to a desorption tower, and drying, filtering and the like to obtain the required LPG mixed space.
Example 5
Step one, mixing propane and butane according to a ratio of 5:5 to form mixed gas A; mixing (propane and butane) with air according to a ratio of 6.5:3.5 to form a mixed gas B;
step two, pressurizing the mixed gas A, then respectively entering a mixing tower for mixing, heating the mixed gas to 40 ℃ by using a heater, and then cooling to obtain gas to be hydrogenated; pressurizing the mixed gas B, then respectively mixing the mixed gas B with a mixing tower, heating the mixed gas to 45 ℃ by using a heater, and then cooling to obtain the prefabricated LPG;
introducing the prefabricated gas and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction; the reaction temperature is regulated to 60 ℃, the reaction pressure is regulated to 0.2Mpa, and the duration time is regulated to 2 hours;
step four, the gas after hydrogenation reaction is further mixed with the prefabricated LPG, so that the mixing volume of the gas after hydrogenation reaction is the same as the volume of the prefabricated LPG, and LPG mixing space is formed; and (3) conveying the LPG mixed space to a desorption tower, and drying, filtering and the like to obtain the required LPG mixed space.
Table 1 examples 1-5 process parameters
In order to verify that the LPG mix prepared in the embodiment of the present invention has a good conversion rate, the LPG mix preparation process for replacing natural gas provided in the embodiment of the present invention will be described by the following test examples.
Test example: experiments on the combustion heat value of the LPG mixture provided in examples 1-5 of the present invention were performed, and the conversion rate of the LPG mixture was provided, specifically Table 2;
according to the LPG empty mixing preparation process provided by the embodiments 1-5 of the invention, the average conversion rate is 90.02%, which shows that the conversion rate is higher, and the energy cost can be effectively reduced by adopting the process of the invention; heat of combustionAverage value of 46.85MJ/m 3 The combustion heat value of the LPG is obviously stronger than that of natural gas, so that the LPG air mixing prepared by the invention can be used for replacing the natural gas and is superior to the natural gas.
The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the above-described embodiments, and that the above-described embodiments and descriptions are only preferred embodiments of the present invention, and are not intended to limit the invention, and that various changes and modifications may be made therein without departing from the spirit and scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (7)
1. An LPG mixing space preparation process for replacing natural gas, characterized by comprising the following steps:
s1, mixing propane and butane according to a proportion to form a mixed gas A; mixing propane, butane and air in proportion to form mixed gas B for preparing LPG prefabricated mixed air;
s2, pressurizing the mixed gas A, then respectively entering a mixing tower for mixing, heating the mixed gas by using an energy-saving heater, and then cooling to obtain gas to be hydrogenated; pressurizing the mixed gas B, then respectively entering a mixing tower for mixing, heating the mixed gas by a heater, and then cooling to obtain the prefabricated LPG;
s3, introducing the prefabricated LPG and hydrogen into a low-temperature plasma reactor through a compressor to carry out a hydrogen gasification reaction, and after the mixed gas enters the low-temperature plasma reactor, breaking chemical bonds in molecules through the excitation of plasma to further carry out a hydrogenation reaction to generate methane and ethane;
s4, further mixing the gas after the hydrogenation reaction with the prefabricated LPG to enable the mixing volume of the gas after the hydrogenation reaction to be the same as the volume of the prefabricated LPG, so as to form LPG mixing space;
in the S1, the mixing volume ratio of propane to butane in the mixed gas A is 6-7:4-3;
in the step S1, the mixing volume ratio of propane and butane in the mixed gas B to air is 5-6:5-4;
in the step S3, the hydrogenation reaction temperature is 60-80 ℃, the reaction pressure is 0.1-0.2Mpa, and the duration is 1-2h.
2. The LPG mix air preparation process for replacing natural gas according to claim 1, characterized in that: in the step S2, the gas heating temperature after mixing the mixed gas A is 25-45 ℃.
3. The LPG mix air preparation process for replacing natural gas according to claim 1, characterized in that: in the step S2, the heating temperature of the gas obtained by mixing the mixed gas B is 35-45 ℃.
4. The LPG mix air preparation process for replacing natural gas according to claim 1, characterized in that: in the step S2, the mixing equipment mainly comprises a mixing machine, and is provided with a mixing fan blade system and a packing layer.
5. The LPG mix air preparation process for replacing natural gas according to claim 1, characterized in that: in the step S2, the heater is preferably an energy-saving heater.
6. The LPG mix air preparation process for replacing natural gas according to claim 1, characterized in that: in the step S2, the pressurizing treatment adopts a multi-stage pressurizing mode.
7. The LPG mix air preparation process for replacing natural gas according to claim 1, characterized in that: in the step S4, after the LPG mixing space is formed, the LPG mixing space is sent to a desorption tower, and the required LPG mixing space can be obtained through drying and filtering treatment.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202310525812.7A CN116554928B (en) | 2023-05-11 | 2023-05-11 | LPG air mixing preparation process for replacing natural gas |
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| CN202310525812.7A CN116554928B (en) | 2023-05-11 | 2023-05-11 | LPG air mixing preparation process for replacing natural gas |
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| CN116554928A CN116554928A (en) | 2023-08-08 |
| CN116554928B true CN116554928B (en) | 2023-12-22 |
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| FR2889292B1 (en) * | 2005-07-26 | 2015-01-30 | Optimise | METHOD AND INSTALLATION FOR COMBUSTION WITHOUT SUPPORT OF POOR COMBUSTIBLE GAS USING A BURNER AND BURNER THEREFOR |
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