CN113173565A - Production process for preparing laughing gas by using continuous flow microchannel reactor - Google Patents
Production process for preparing laughing gas by using continuous flow microchannel reactor Download PDFInfo
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- CN113173565A CN113173565A CN202110498448.0A CN202110498448A CN113173565A CN 113173565 A CN113173565 A CN 113173565A CN 202110498448 A CN202110498448 A CN 202110498448A CN 113173565 A CN113173565 A CN 113173565A
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- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 title claims abstract description 118
- 235000013842 nitrous oxide Nutrition 0.000 title claims abstract description 54
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 35
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 claims abstract description 94
- 238000000034 method Methods 0.000 claims abstract description 40
- 230000008569 process Effects 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 229910001868 water Inorganic materials 0.000 claims abstract description 22
- 239000007787 solid Substances 0.000 claims abstract description 14
- 239000002994 raw material Substances 0.000 claims abstract description 10
- 238000002360 preparation method Methods 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 58
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 16
- 239000000203 mixture Substances 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 7
- 238000007670 refining Methods 0.000 claims description 7
- 229910021529 ammonia Inorganic materials 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 239000000112 cooling gas Substances 0.000 claims description 3
- 239000012071 phase Substances 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims 1
- 238000001816 cooling Methods 0.000 abstract description 8
- 238000002844 melting Methods 0.000 abstract description 4
- 230000008018 melting Effects 0.000 abstract description 4
- 150000001875 compounds Chemical class 0.000 abstract description 3
- 239000003337 fertilizer Substances 0.000 abstract description 3
- 238000003860 storage Methods 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 description 10
- 239000000463 material Substances 0.000 description 9
- 238000000354 decomposition reaction Methods 0.000 description 4
- 230000004907 flux Effects 0.000 description 4
- 239000001272 nitrous oxide Substances 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000003444 anaesthetic effect Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000003745 diagnosis Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
- C01B21/22—Nitrous oxide (N2O)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
Abstract
The invention relates to the technical field of production processes for preparing laughing gas by decomposing ammonium nitrate, in particular to a production process for preparing laughing gas by using a continuous flow microchannel reactor. The process comprises the steps of 1) preparing raw materials, namely preparing an ammonium nitrate solution by taking an ammonium nitrate solution or solid ammonium nitrate as the raw materials; 2) reaction preparation, namely feeding an ammonium nitrate solution into a microchannel reactor for reaction, and decomposing ammonium nitrate to generate laughing gas and water; 3) gas-liquid separation; 4) and (5) cooling the gas. The laughing gas production process can be used for co-production with industrial ammonium nitrate and compound fertilizer in a factory, the ammonium nitrate solution is conveyed by a pipeline, the transportation cost is saved, 92-95% of ammonium nitrate solution is directly adopted, steam for melting can be saved, the cost is reduced, the transportation and storage cost of solid ammonium nitrate is further saved, the cost is reduced, and the safety is improved.
Description
Technical Field
The invention relates to the technical field of production processes for preparing laughing gas by decomposing ammonium nitrate, in particular to a production process for preparing laughing gas by using a continuous flow microchannel reactor.
Background
Nitrous oxide, formula N2And O. It is also called laughing gas, a colorless and sweet gas, an oxidant, and can support combustion under certain conditions (with oxygen because laughing gas is at high temperatureCapable of decomposing into nitrogen and oxygen), but stable at room temperature, has mild anesthetic effect, and can cause laughing.
Nitrous oxide was discovered in 1772 in joseph priestly. They found that nitrous oxide was capable of depriving the patient of pain and that after inhalation, consciousness was maintained and not confused. Laughing gas is used as an anesthetic soon, especially in the field of dentists. Since a dentist does not usually have a professional anesthesiologist, and the patient is required to keep clear-headed and can make oral reaction according to the order in the diagnosis and treatment process, the gas brings great convenience to the dentist.
At present, the process for preparing laughing gas by utilizing ammonium nitrate pyrolysis is the main process for producing laughing gas at present, and the main flow of the process is to convey ammonium nitrate (solid or liquid ammonium nitrate) to a stirring reaction kettle with a coil pipe or a jacket by utilizing a pump, heat the ammonium nitrate in the reaction kettle to 220 ℃, and decompose the ammonium nitrate into laughing gas and water.
The existing ammonium nitrate heating kettle is a common stirring type reaction kettle, the reaction pressure is normal pressure, the temperature is 220 ℃, the operation condition is severe in the reaction process, the operation is unstable, the operation elasticity is small, heating dead angles are easy to occur, the local overheating of ammonium nitrate is caused, the violent decomposition of the ammonium nitrate is caused, and further the explosion is caused. Meanwhile, due to the heating reaction process, materials cause serious corrosion to common metal materials, potential equipment safety hazards are caused, and the manufacturing cost of adopting rare metals is also extremely high.
Disclosure of Invention
The invention aims to overcome the problems of low safety coefficient and high danger in the prior industrial production of laughing gas, and provides a production process for preparing laughing gas by using a continuous flow microchannel reactor.
In order to achieve the above purpose, the specific technical scheme of the invention is as follows:
a production process for preparing laughing gas by using a continuous flow microchannel reactor comprises the following steps:
(1) preparing raw materials: adding ammonium nitrate solution or solid ammonium nitrate and water into a stirring kettle with a coil pipe, and introducing steam into the coil pipe to melt the ammonium nitrate.
As a preferred embodiment of the present invention, the temperature in the stirred tank is maintained at 120 to 130 ℃.
(2) Reaction preparation: and (2) sending the ammonium nitrate solution formed in the step (1) into a micro-channel reactor with a heating chip and a cooling chip, and reacting at a certain temperature to decompose the ammonium nitrate to generate laughing gas and water.
As a better implementation mode in the application, the reaction conditions in the microchannel reactor are normal pressure and the temperature is 220-225 ℃; more preferably 220 deg.c.
(3) Gas-liquid separation: and (3) sending the gas-liquid mixture obtained in the step (2) into a process gas pre-cooler, reducing the temperature of the gas to saturation temperature, and then sending the gas-liquid mixture into a separator to separate the gas phase from the liquid phase.
As a preferred embodiment in this application, the temperature of the gas-liquid mixture in the process gas pre-cooler is reduced to about 100-.
(4) Cooling gas: and (4) introducing the mixed gas from the separator into a process gas cooler, reducing the temperature of the gas to 40-50 ℃, and sending the cooled gas to a post-working section for refining.
As a preferred embodiment in the present application, the liquid phase separated in step (3) is an unreacted ammonium nitrate solution, which is refluxed to the stirred tank in step (1) and mixed with fresh ammonium nitrate to prepare a new solution; the gas mixture containing laughing gas and water vapor is sent to a post-stage for refining.
As a better embodiment in the application, the mass percentage of the ammonium nitrate solution is 92-95%, the ammonium nitrate solution can be directly adopted, or solid ammonium nitrate is added with water and heated to be melted to prepare 92-95% ammonium nitrate solution;
according to the production process for preparing laughing gas by using the continuous flow microchannel reactor, in the step (3), the mass content of laughing gas in the gas mixture is 50-55%, the mass content of water vapor is 45-50%, other gases such as 2% of nitrogen, trace NOX gas and ammonia are contained, and the sum of the total volume percentage of all gases is 100%.
As a better implementation mode in the application, the production process for preparing laughing gas by using the continuous flow microchannel reactor comprises the steps of adding 92-95% ammonium nitrate solution prepared by taking ammonium nitrate as a raw material into the microchannel reactor, heating to 220 ℃, and decomposing the ammonium nitrate at the temperature to generate laughing gas and water.
The reaction formula for producing laughing gas is as follows:
NH4NO3——N2O↑+2H2O↑
the micro-channel reactor adopted by the laughing gas production process is a continuous flow pipeline reactor, the continuous flow pipeline reactor consists of a plurality of reaction plates, each plate is provided with a reaction channel, the diameter of the reaction channel is generally in a micrometer and millimeter level, each plate can be provided with a plurality of material inlets and material outlets according to requirements, the outlet of the previous plate is connected with the inlet of the next plate, and both sides of each reaction plate can be provided with heat exchange plates for regulating and controlling the temperature of a reaction system. Compared with the traditional gap type stirred tank reactor, the microchannel reactor has the advantages of high mass transfer and heat transfer efficiency, accurate control of reaction temperature, raw material proportion and reaction time, safe and reliable reaction operation, great reduction or even complete elimination of side reaction and the like. Meanwhile, the production safety can be ensured to the greatest extent by utilizing the characteristic that the liquid holdup of the microchannel reactor is extremely low.
Furthermore, the laughing gas production process can be used for co-production with industrial ammonium nitrate and compound fertilizer in a factory, and the ammonium nitrate solution is conveyed by adopting a pipeline, so that the transportation cost is saved. And if the 92-95% ammonium nitrate solution is directly adopted, the steam for melting can be saved, the production cost is reduced, the transportation and storage cost of solid ammonium nitrate is further saved, the cost is reduced, and the safety is improved.
Compared with the prior art, the invention has the beneficial effects that:
the safety factor is high, the extremely low liquid holdup of the microchannel reactor is utilized, the production safety is ensured to the maximum extent, the accurate control of reaction conditions is ensured by good heat transfer and mass transfer, the reaction is more thorough, the side reaction is less, and the maximum yield is ensured.
And (II) the cost is low, the heat and mass transfer is good, the optimal heat transfer effect is ensured, and the steam consumption is reduced.
And (III) the corrosion resistance is high, the reaction plate is made of materials with high corrosion resistance, the size of a single reaction plate is usually not more than 500mm x 500mm, and the material consumption is reduced, so that the equipment purchase cost is reduced.
(IV) production continuity: the micro-channel reactor can realize continuous production of preparing laughing gas.
Description of the drawings:
FIG. 1 is a flow chart of the process for producing laughing gas using a continuous flow microchannel reactor according to the present invention.
FIG. 2 is a schematic structural view of a microchannel reactor
Detailed Description
A production process for preparing laughing gas by using a continuous flow microchannel reactor comprises the following steps:
(1) preparing raw materials: adding ammonium nitrate solution or solid ammonium nitrate and water into a stirring kettle with a coil pipe, introducing steam into the coil pipe to melt the ammonium nitrate, and keeping the temperature in the kettle between 120 and 130 ℃.
(2) Reaction preparation: sending the ammonium nitrate solution formed in the step (1) into a micro-channel reactor with a heating chip and a cooling chip, reacting at the temperature of 220-225 ℃, and decomposing the ammonium nitrate to generate laughing gas and water;
(3) gas-liquid separation: and (3) sending the gas-liquid mixture obtained in the step (2) into a process gas pre-cooler, reducing the temperature of the gas to saturation temperature, and then sending the gas-liquid mixture into a separator to separate the gas phase from the liquid phase.
(4) Cooling gas: and (4) introducing the mixed gas from the separator into a process gas cooler, reducing the temperature of the gas to 40-50 ℃, and sending the cooled gas to a post-working section for refining.
The liquid phase separated in the step (3) is an unreacted ammonium nitrate solution, and the unreacted ammonium nitrate solution is refluxed to the stirring kettle in the step (1) and mixed with fresh ammonium nitrate to prepare a new solution; sending a gas mixture containing laughing gas and water vapor to a post-working section for refining;
the mass percentage of the ammonium nitrate solution is 92-95%, the ammonium nitrate solution can be directly adopted, or solid ammonium nitrate is added with water and heated to be melted to prepare 92-95% ammonium nitrate solution;
according to the production process for preparing laughing gas by using the continuous flow microchannel reactor, in the step (3), the mass content of laughing gas in the gas mixture is 50-55%, the mass content of water vapor is 45-50%, other gases such as 2% of nitrogen, trace NOX gas and ammonia are contained, and the sum of the total volume percentage of all gases is 100%.
In the production process for preparing laughing gas, the reaction condition in the step (2) is normal pressure.
A production process for preparing laughing gas by using a continuous flow microchannel reactor is characterized in that 92-95% ammonium nitrate solution prepared by taking ammonium nitrate as a raw material is added into the microchannel reactor, the temperature is increased to 220 ℃, and the ammonium nitrate is decomposed at the temperature to generate laughing gas and water.
The reaction formula for producing laughing gas is as follows:
NH4NO3——N2O↑+2H2O↑
the micro-channel reactor adopted by the laughing gas production process is a continuous flow pipeline reactor, the continuous flow pipeline reactor is composed of more than 4 reaction plate sheets, each plate is provided with a reaction channel, the diameter of the reaction channel is 0.1-10 mm, each plate sheet can be provided with 2 material inlets and 1 outlet according to requirements, the outlet of the previous plate sheet is connected with the inlet of the next plate sheet, and both sides of each reaction plate sheet can be provided with heat exchange plate sheets for regulating and controlling the temperature of a reaction system.
Furthermore, the laughing gas production process can be used for co-production with industrial ammonium nitrate and compound fertilizer in a factory, and the ammonium nitrate solution is conveyed by adopting a pipeline, so that the transportation cost is saved. And if the 92-95% ammonium nitrate solution is directly adopted, the steam for melting can be saved, the production cost is reduced, the transportation and storage cost of solid ammonium nitrate is further saved, the cost is reduced, and the safety is improved.
In order to facilitate the understanding of the present invention, the process described in the present invention will be further described with reference to the accompanying drawings and the detailed description. It should not be understood that the scope of the above-described subject matter of the present invention is limited to the following examples.
Example 1:
a production process for preparing laughing gas by using a continuous flow microchannel reactor comprises the following steps:
(a) solid ammonium nitrate is used as a raw material, and the annual yield is 1000 tons of laughing gas;
(b) firstly, 1950 tons of ammonium nitrate are added into 100 tons of water to prepare ammonium nitrate solution with the mass concentration of 95 percent, and the mass is 2050 tons;
(c) and (c) conveying the ammonium nitrate solution obtained in the step (b) to a micro-channel reactor through a pump, maintaining the reaction temperature of the reactor at 220-225 ℃ through an external heating source, and decomposing the ammonium nitrate into laughing gas and water with the yield of 98-99%. The reactor flux per hour is 280kg, the liquid holdup of a 2000-ton reactor per year flux is only 1L, and the retention time is 1-2 minutes;
d) introducing the gas mixture containing a large amount of laughing gas and water generated in the step (c) into a process gas precooler, and reducing the temperature to 110-115 ℃;
(e) the mixed gas out of the process precooler enters a separator to separate and trap the unreacted and sufficient ammonium nitrate; the separated ammonium nitrate solution returns to the ammonium nitrate preparation tank and is mixed with solid ammonium nitrate to prepare a new ammonium nitrate solution;
(f) and (e) introducing the laughing gas-rich mixed gas obtained from the separator in the step (e) into a process gas cooler, cooling the mixed gas to 40-50 ℃ by using circulating water, sending the cooled gas to a post-working section for refining, and removing water, ammonia, nitrogen and other impurity gases to meet different product quality requirements.
Example 2:
a production process for preparing laughing gas by using a continuous flow microchannel reactor comprises the following steps:
(a) ammonium nitrate solution with the mass concentration of 95 percent directly produced by a factory is taken as a raw material, the temperature is about 125 ℃, and the annual output is 1000 tons of laughing gas;
(b) the 95% concentration ammonium nitrate solution prepared in the original process is conveyed to a microchannel reactor through a pump, the ammonium nitrate solution is heated to 220-225 ℃ in the reactor, ammonium nitrate is decomposed into laughing gas and water, the yield is about 98-99%, the yield is not changed, but the components of the product are different because of gaseous ammonia in the ammonium nitrate solution in a factory. The hourly flux of the reactor is still 280kg, the annual flux is about 1L of the liquid holdup of 2000 tons of reactor, and the retention time is 1-2 minutes;
(d) introducing the gas mixture containing a large amount of laughing gas and water generated in the step (c) into a process gas precooler, and reducing the temperature to 110-115 ℃;
(e) the mixed gas out of the process precooler enters a separator to separate and trap the unreacted and sufficient ammonium nitrate; the separated ammonium nitrate solution returns to the ammonium nitrate preparation tank and is mixed with solid ammonium nitrate to prepare a new ammonium nitrate solution;
(f) and (e) introducing the laughing gas-rich mixed gas obtained from the separator in the step (e) into a process gas cooler, cooling the mixed gas to about 45 ℃ by using circulating water, sending the cooled gas to a post-working section for refining, and removing water, ammonia, nitrogen and other impurity gases to meet different product quality requirements.
Comparative example 1:
in the traditional production process, solid ammonium nitrate and water with the concentration of about 7 percent are added into a melting pot to be heated, the temperature is controlled to 130 ℃ to melt the ammonium nitrate, and a circulating pump is arranged in the pot to ensure that the temperature of materials in the pot is uniform. The melted ammonium nitrate is pumped into a tubular or kettle type reactor through a pump to react, and the temperature is rapidly raised to 220 ℃ to generate crude nitrous oxide and water vapor. The volume of a common reaction kettle is about 500L, a heating coil and a stirrer are arranged in the reaction kettle, heat and mass transfer is slow, ammonium nitrate is easy to generate side decomposition reaction, so that the utilization of the ammonium nitrate is reduced, the reaction yield is usually lower than 95%, the heat and mass transfer capacity of the microchannel reactor is 100-1000 times higher than that of the traditional equipment, the back flow is reduced, and the yield reaches more than 99%. Ammonium nitrate in the reaction kettle is decomposed into laughing gas through continuous heating and stirring, the whole reaction time is about 1 hour, and the safety risk is increased. Most of manufacturers adopting the traditional process adopt intermittent operation, the automation degree is low, the manual operation is large, and meanwhile, the production safety limits the improvement of the productivity, compared with the micro-channel reactor, the automatic control and the remote control can be realized, and the amplification effect cannot be caused by the improvement of the productivity of the device.
From the safety perspective, the liquid holdup of the tubular reactor with the same yield is one thousandth of the liquid holdup of the microchannel reactor, once the reaction process is abnormal, the cooling speed and the cooling effect of the tubular reactor and the kettle type reactor are far lower than those of the microchannel reactor, and the harm caused by the higher liquid holdup and the untimely cooling is far higher than that of the microchannel reactor. The liquid holdup of the microchannel reactor is only 1kg, the heat and mass transfer capacity is strong, the temperature is rapidly reduced, the materials are not easy to overheat, and the safety of ammonium nitrate decomposition reaction is greatly ensured.
As can be seen from the comparison of example 1, example 2 and comparative example 1, because the conventional process adopts a stirring kettle, the ammonium nitrate is decomposed to generate laughing gas by continuous heating and stirring, but the ammonium nitrate is easy to generate violent decomposition and explosion at high temperature, and the production process is very dangerous. The microchannel reactor is a reactor with small liquid holdup and high heat exchange efficiency, the temperature control is stable, the materials are not easy to overheat, and the low liquid holdup ensures that the consequence caused by accidents is very small and the safety is high.
The above embodiments are only used for illustrating the technical solutions of the present patent, and not for limiting the same; although the present patent is described in detail with reference to the foregoing embodiments, those of ordinary skill in the art will understand that: the technical solutions described in the foregoing embodiments can be modified, or some technical features can be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the spirit and scope of the technical solutions of the embodiments of the present patent.
Claims (9)
1. A production process for preparing laughing gas by using a continuous flow microchannel reactor is characterized by comprising the following steps:
(1) preparing raw materials: adding ammonium nitrate solution or solid ammonium nitrate and water into a stirring kettle with a coil pipe, and introducing steam into the coil pipe to melt the ammonium nitrate;
(2) reaction preparation: sending the ammonium nitrate solution formed in the step (1) into a microchannel reactor, reacting at 220-225 ℃, and decomposing ammonium nitrate to generate laughing gas and water;
(3) gas-liquid separation: sending the gas-liquid mixture obtained in the step (2) into a process gas pre-cooler, reducing the temperature of the gas to saturation temperature, and then sending the gas-liquid mixture into a separator to separate the gas phase and the liquid phase;
(4) cooling gas: and the mixed gas from the separator enters a process gas cooler, and the cooled gas is sent to a post-working section for refining.
2. The process of claim 1, wherein the process comprises: and (4) refluxing the liquid phase separated in the step (3) to the stirring kettle in the step (1) to be mixed with fresh ammonium nitrate to prepare an ammonium nitrate solution, wherein the liquid phase is an unreacted and sufficient ammonium nitrate solution.
3. The process of claim 1, wherein the process comprises: the mass concentration of the ammonium nitrate solution sent into the microchannel reactor is 92-95 percent.
4. The process of claim 1, wherein the process comprises: in the step (1), the temperature in the kettle is required to be kept between 120 and 130 ℃.
5. The process of claim 1, wherein the process comprises: and (4) after the gas mixture in the step (3) is sent into a process gas precooler, reducing the temperature to 100-115 ℃.
6. The process of claim 1, wherein the process comprises: in the step (4), the mass content of laughing gas in the mixed gas from the separator is 50-55%, the mass content of water vapor is 45-50%, the balance is other gases, and the sum of the total volume percentage is 100%.
7. The process of claim 1, wherein the process comprises: and (4) introducing the mixed gas in the step (4) into a process gas cooler to reduce the temperature of the gas to 40-50 ℃.
8. The process of claim 1, wherein the process comprises: the microchannel reactor is a continuous flow pipeline reactor, and the diameter of the channel is micron-sized or millimeter-sized.
9. The process of claim 6, wherein the process comprises: the other gases are nitrogen, a trace amount of NOX gas and ammonia.
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| CN112138615A (en) * | 2020-10-14 | 2020-12-29 | 北京万机汇机电工程技术有限公司 | Preparation device and method of nitrous oxide |
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Application publication date: 20210727 |