CN117163919B - Hydrogen production system and method based on ammonia - Google Patents
Hydrogen production system and method based on ammonia Download PDFInfo
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- CN117163919B CN117163919B CN202311444122.5A CN202311444122A CN117163919B CN 117163919 B CN117163919 B CN 117163919B CN 202311444122 A CN202311444122 A CN 202311444122A CN 117163919 B CN117163919 B CN 117163919B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 228
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 95
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 58
- 239000001257 hydrogen Substances 0.000 title claims abstract description 57
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 20
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 claims abstract description 96
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 83
- XMBWDFGMSWQBCA-UHFFFAOYSA-N hydrogen iodide Chemical compound I XMBWDFGMSWQBCA-UHFFFAOYSA-N 0.000 claims abstract description 83
- 239000007789 gas Substances 0.000 claims abstract description 74
- 229910000043 hydrogen iodide Inorganic materials 0.000 claims abstract description 72
- XZXYQEHISUMZAT-UHFFFAOYSA-N 2-[(2-hydroxy-5-methylphenyl)methyl]-4-methylphenol Chemical compound CC1=CC=C(O)C(CC=2C(=CC=C(C)C=2)O)=C1 XZXYQEHISUMZAT-UHFFFAOYSA-N 0.000 claims abstract description 66
- 229940107816 ammonium iodide Drugs 0.000 claims abstract description 66
- 239000007787 solid Substances 0.000 claims abstract description 57
- 238000006243 chemical reaction Methods 0.000 claims abstract description 53
- 238000003860 storage Methods 0.000 claims abstract description 43
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 claims abstract description 41
- 229910052740 iodine Inorganic materials 0.000 claims abstract description 41
- 239000011630 iodine Substances 0.000 claims abstract description 41
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000007132 Bunsen reaction Methods 0.000 claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000002245 particle Substances 0.000 claims abstract description 14
- 238000005516 engineering process Methods 0.000 claims abstract description 11
- 238000002156 mixing Methods 0.000 claims abstract description 6
- 238000001035 drying Methods 0.000 claims abstract description 3
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 40
- QPBYLOWPSRZOFX-UHFFFAOYSA-J tin(iv) iodide Chemical compound I[Sn](I)(I)I QPBYLOWPSRZOFX-UHFFFAOYSA-J 0.000 claims description 21
- DLYUQMMRRRQYAE-UHFFFAOYSA-N tetraphosphorus decaoxide Chemical compound O1P(O2)(=O)OP3(=O)OP1(=O)OP2(=O)O3 DLYUQMMRRRQYAE-UHFFFAOYSA-N 0.000 claims description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 18
- 229910052760 oxygen Inorganic materials 0.000 claims description 18
- 239000001301 oxygen Substances 0.000 claims description 18
- 238000000354 decomposition reaction Methods 0.000 claims description 13
- 239000000243 solution Substances 0.000 claims description 13
- 239000007864 aqueous solution Substances 0.000 claims description 11
- 230000004888 barrier function Effects 0.000 claims description 11
- 229940071870 hydroiodic acid Drugs 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 150000002431 hydrogen Chemical class 0.000 claims description 7
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- 230000008929 regeneration Effects 0.000 claims description 5
- 238000011069 regeneration method Methods 0.000 claims description 5
- PMJHPLYNASCEAT-UHFFFAOYSA-N [Sn].[I] Chemical compound [Sn].[I] PMJHPLYNASCEAT-UHFFFAOYSA-N 0.000 claims description 4
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 4
- 239000000292 calcium oxide Substances 0.000 claims description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 4
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- 239000011259 mixed solution Substances 0.000 claims description 2
- 238000001816 cooling Methods 0.000 abstract description 6
- 238000004064 recycling Methods 0.000 abstract description 6
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 abstract description 5
- 229910001873 dinitrogen Inorganic materials 0.000 abstract description 5
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 18
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 10
- 229910021536 Zeolite Inorganic materials 0.000 description 10
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- 239000010457 zeolite Substances 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 8
- 239000002994 raw material Substances 0.000 description 6
- 238000005979 thermal decomposition reaction Methods 0.000 description 6
- GOIGHUHRYZUEOM-UHFFFAOYSA-N [S].[I] Chemical compound [S].[I] GOIGHUHRYZUEOM-UHFFFAOYSA-N 0.000 description 5
- 239000001569 carbon dioxide Substances 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 229910000039 hydrogen halide Inorganic materials 0.000 description 4
- 239000012433 hydrogen halide Substances 0.000 description 4
- 238000011065 in-situ storage Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 230000002194 synthesizing effect Effects 0.000 description 4
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 3
- 229910006404 SnO 2 Inorganic materials 0.000 description 3
- -1 ammonium halide Chemical class 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910020630 Co Ni Inorganic materials 0.000 description 2
- 229910002440 Co–Ni Inorganic materials 0.000 description 2
- 238000009620 Haber process Methods 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010494 dissociation reaction Methods 0.000 description 2
- 230000005593 dissociations Effects 0.000 description 2
- 229910052736 halogen Inorganic materials 0.000 description 2
- 150000002367 halogens Chemical class 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 239000012024 dehydrating agents Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
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- Catalysts (AREA)
Abstract
The application relates to the field of energy utilization, in particular to a hydrogen production system and a method based on ammonia, which comprise the steps of carrying out a bunsen reaction, preparing hydrogen iodide gas, carrying out a plasma reaction to prepare ammonium iodide, using a low-temperature plasma technology to enable the hydrogen iodide gas and nitrogen gas to react to obtain mixed gas containing ammonium iodide particles, iodine steam, the hydrogen iodide gas and nitrogen gas, then carrying out gas-solid separation to obtain ammonium iodide solid, mixing the ammonium iodide solid with tin dioxide solid, heating, decomposing the ammonium iodide into ammonia gas and hydrogen iodide, carrying out a reaction between the hydrogen iodide and the tin dioxide to generate tetraiodide and water, cooling the mixed gas containing the ammonia gas, the tetraiodide and the water to 473K-623K, separating the tetraiodide gas liquefaction, and drying the mixed gas containing the ammonia gas and the water vapor, and cooling or carrying out pressurized liquefaction to obtain liquid ammonia for storage and transportation. According to the method, ammonia is prepared by decomposing ammonium iodide through a plasma reaction mode by recycling tin element, and the reaction efficiency is improved on the premise that ammonia is easy to transport.
Description
Technical Field
The present application relates to the field of energy utilization, and in particular to an ammonia-based hydrogen production system and method.
Background
The hydrogen energy is a recognized renewable clean energy, and the hydrogen production method of thermochemical sulfur-iodine cycle (hereinafter referred to as sulfur-iodine cycle) mainly comprises Bunsen reaction and sulfuric acid H 2 SO 4 Three schemes of decomposition and hydrogen iodide HI decomposition. The sulfur iodine cycle has many unique advantages, such as: (1) compared with direct thermal decomposition of water to produce hydrogen, the reaction condition is relatively mild, and the heat sources such as solar energy, nuclear energy and the like can be matched; (2) the hydrogen production heat efficiency is high; (3) without oxyhydrogenThe separation device is suitable for large-scale hydrogen production. However, when the sulfur-iodine hydrogen production system is matched with high-quality green heat sources such as solar energy, nuclear energy and the like, certain regional limitations are likely to exist in the sulfur-iodine hydrogen production technology, so that the technology has the difficult problems of hydrogen storage and transportation after large-scale hydrogen production is realized. An effective solution to the above problems is to convert hydrogen into other substances that are easy to transport over long distances.
For example, chinese patent application publication No.: CN116199562a, name: method and system for preparing methanol by combining carbon dioxide and hydrogen iodide, which discloses I generated by decomposing hydrogen iodide gas 2 And H 2 And (3) simultaneously introducing carbon dioxide required by preparing methanol with HI as a mixed gas A in a corresponding proportion, controlling the temperature of the carbon dioxide to ensure that the carbon dioxide is mixed with the mixed gas A, introducing the mixed gas A into a methanol synthesizer, and introducing the mixed gas obtained by reaction into a cooling separation process to obtain methanol. The application utilizes the reaction of synthesizing methanol to consume hydrogen generated by the decomposition of hydroiodic acid in situ, thereby promoting the hydrogen production and the decomposition of hydrogen iodide; meanwhile, the hydrogen is directly converted into methanol which is easy to store and transport at normal temperature and normal pressure, so that the cost and technical difficulty of hydrogen storage and transportation are reduced.
For example, chinese patent publication No.: CN114772551B, name: a method and system for efficient utilization of methane-rich gas, which discloses the use of nitrogen and H generated by air separation 2 The synthesized ammonia gas product can be used as chemical raw material, and can be liquefied into liquid ammonia for long-distance transportation. Liquid ammonia as H 2 Chemical carrier for long distance (more than or equal to 200 km) transportation to solve H 2 And the problem of difficult transportation in a long distance (more than or equal to 200 km) is solved. However, current industrial synthesis of ammonia is mainly achieved by the Haber-Bosch process. The Haber process generally requires high temperatures and pressures and the presence of an iron/ruthenium based catalyst to produce nitrogen and hydrogen H 2 The reaction is converted into ammonia gas, and the high temperature and high pressure lead to quite high energy consumption for preparing the ammonia gas. Additional raw material H 2 Mainly obtained by methane steam reforming, which consumes fossil energy and generates a large amount of greenhouse gases.
For another example, japanese patent laid-open No.: JP5660493B2, name: a method for synthesizing ammonia by thermochemical cycle is disclosed, which uses nitrogen and water as raw materials and renewable energy as energy. The reaction of nitrogen and hydrogen halide is carried out by the circulation of ammonium halide in a thermodynamic mode, specifically, the reaction temperature is controlled to be 323K-523K under the existence of a metal catalyst, the reaction pressure is controlled to be 0.05 MPa-2.0 MPa, and the nitrogen and the hydrogen halide are reacted to generate the ammonium halide and a halogen simple substance; then under the condition of 573K-873K and 0.05 MPa-1.0 MPa, the ammonia halide is thermally decomposed into ammonia gas and hydrogen halide; ammonia gas is then separated by adsorption using zeolite, thereby producing ammonia gas. The ammonia is synthesized by a step of reacting ammonia with hydrogen halide to obtain ammonia and a step of recycling byproduct halogen without auxiliary raw materials. However, this method is extremely inefficient in the production of ammonia, and, taking example 7 thereof as an example, only 0.43mol% nitrogen and 0.139mol% hydrogen iodide gas can be converted using a 5wt% Pt catalyst. In addition, the mentioned zeolite, particularly USY zeolite or modified USY zeolite, is difficult to resist corrosion of hydrogen iodide gas at high temperature, has short service life and low separation efficiency, so that the technical route still has a plurality of problems and has a large lifting space.
Disclosure of Invention
Aiming at the technical problems in the prior art, the application provides a novel hydrogen production system and method based on ammonia, which are used for preparing ammonia which is easy to transport for a long distance through high-efficiency reaction.
On one hand, the application provides a hydrogen production method based on ammonia, which comprises the steps of S1, carrying out a bunsen reaction, layering a bunsen reaction solution to obtain a hydroiodic acid aqueous solution, preparing S2 hydrogen iodide gas, and mixing the hydroiodic acid aqueous solution with phosphorus pentoxide to obtain hydrogen iodide gas; s3, performing plasma reaction to prepare ammonium iodide, and reacting nitrogen with hydrogen iodide gas of S2 by using a low-temperature plasma technology to obtain mixed gas A; s4, gas-solid separation, wherein the temperature of the mixed gas A of S3 is kept higher than 458K, and the ammonium iodide solid is obtained through the first gas-solid separation; and/or the residual mixed gas B of the first gas-solid separation is cooled to 293K-313K, the second gas-solid separation is carried out, the obtained elemental iodine is sent to an elemental iodine storage tank, and the residual mixed gas C is sent back to S3 for continuing the plasma reaction; s5, decomposing ammonium iodide and reacting tin iodine, mixing and heating the ammonium iodide solid obtained by S4 and the tin dioxide solid, and reacting hydrogen iodide generated by decomposing the ammonium iodide with the tin dioxide to obtain a mixed gas D; s6, ammonia storage and transportation, wherein the mixed gas D in S5 is cooled to 473K-623K, the tin tetraiodide gas is liquefied and separated, and the rest mixed gas is cooled or pressurized and liquefied into liquid ammonia after being dried; s7, decomposing ammonia to prepare hydrogen, and decomposing ammonia to prepare hydrogen after transporting the liquid ammonia to a destination.
Specifically, the Bunsen reaction solution of S1 is layered to obtain 40-57 wt% aqueous solution of hydroiodic acid, and is fed into S2 to be mixed with phosphorus pentoxide, and the temperature of the mixed solution is controlled to be lower than 573K.
In particular, the molar ratio of the nitrogen to the hydrogen iodide gas in the S3 is 1:6-20, the reaction temperature is 458K-573K, the reaction pressure is 0.1 MPa-10 MPa, and the reaction time is 10 min-120 min.
Particularly, the low-temperature plasma technology is selected from corona discharge, thomson discharge and dielectric barrier discharge, and when the low-temperature plasma technology selects the dielectric barrier discharge, the frequency of the dielectric barrier discharge is 1 kHz-12 kHz, and the input voltage is 1 kV-40 kV.
In particular, in the step S5, the ammonium iodide solid and the tin dioxide solid are mixed, the mixture is heated to 673K-723K, and the decomposition time is 10 min-60 min.
In particular, calcium oxide is used for the drying in S6.
Particularly, the method also comprises the regeneration of tin dioxide, wherein the tin tetraiodide and oxygen in the S6 react under the condition of 673K-773K to generate tin dioxide solid particles and iodine vapor, the tin dioxide solid particles are recycled and then returned to the S5, and the iodine vapor is cooled and sublimated into solid and returned to the S1 circulation to participate in the Bunsen reaction.
In particular, the nitrogen required for S3 and the oxygen required for the regeneration of tin dioxide are produced by an air separator.
On the other hand, the application also provides an ammonia-based hydrogen production system which operates according to the method and comprises a Bunsen reaction tower, a two-phase layering device, a hydrogen iodide generator, a plasma reactor, a gas-solid separator, an ammonium iodide decomposer, a tin dioxide regenerator, an ammonia dryer and an ammonia liquefier which are connected in sequence; the hydrogen iodide generator is also respectively connected with a phosphorus pentoxide storage tank and a phosphoric acid storage tank; the gas-solid separator is also connected with a condensation separator, and the condensation separator is respectively connected with the plasma reactor and the elemental iodine storage tank; the tin dioxide regenerator is also connected with the elemental iodine storage tank and the bunsen reaction tower in sequence, liquefied ammonia can be stored in the ammonia storage tank, so that long-distance transportation is realized, and after the ammonia is transported to a destination, the ammonia is sent into the ammonia decomposer to be decomposed into hydrogen and nitrogen, and finally the preparation of hydrogen is realized.
In particular, the device also comprises an air separator, wherein the air separator is respectively connected with a nitrogen storage tank and an oxygen storage tank, the nitrogen storage tank is connected with the plasma reactor, and the oxygen storage tank is connected with the tin dioxide regenerator.
On the basis of the common sense in the art, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the application.
The technical scheme has the following advantages or beneficial effects: (1) The efficiency of generating ammonium iodide by the reaction of nitrogen and hydrogen iodide is improved in a plasma reaction mode; (2) In the plasma reaction, hydrogen iodide is used as a hydrogen source for synthesizing ammonia, compared with hydrogen, the dissociation energy is lower, the reaction energy consumption is lower, meanwhile, ammonia gas generated by the reaction rapidly reacts with the hydrogen iodide to generate ammonium iodide, the stability of the ammonium iodide is higher than that of the ammonia gas, and the reaction efficiency is ensured; (3) The method has the advantages that tin element is recycled to decompose ammonium iodide to prepare ammonia, tin dioxide and oxygen are used, all ammonium iodide can be almost converted into ammonia at a proper reaction temperature, and compared with a method for separating ammonia by zeolite adsorption, ammonia with higher purity can be obtained by gas-liquid separation, the separation efficiency is higher, and the tin dioxide is recycled and almost has no loss. Of course, not all of the advantages described above are necessarily achieved at the same time by any one of the solutions of the present application.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below. It will be obvious to a person skilled in the art that other figures can be obtained from the figures provided without the inventive effort.
FIG. 1 is a schematic diagram of an ammonia-based hydrogen production system according to one embodiment of the present application.
FIG. 2 is a schematic diagram of an ammonia-based hydrogen production process according to one embodiment of the present application.
Detailed Description
The technical solutions in the embodiments of the present application are clearly and completely described below with reference to the drawings of the present application. It is apparent that the described embodiments are only some of the embodiments of the present application and are intended to be used to explain the inventive concept. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present application without making any inventive effort, are intended to be within the scope of the present application.
The terms "coupled," "connected," and the like as used in the description herein are to be construed broadly and may be, for example, fixedly coupled, detachably coupled, or integrally formed, unless otherwise specifically defined and limited; may be a mechanical connection, an electrical connection; can be directly connected and indirectly connected through an intermediate medium; may be a communication between two elements or an interaction between two elements. The specific meaning of the terms in the embodiments can be understood by those of ordinary skill in the art according to the specific circumstances.
The terms "one particular embodiment" and "one particular embodiment" as used in this description mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present application. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
Referring to fig. 1, one embodiment of the present application proposes an ammonia-based hydrogen production system comprising a bunsen reactor, a two-phase separator, a hydrogen iodide generator, a plasma reactor, a gas-solid separator, an ammonium iodide decomposer, a tin dioxide regenerator, an ammonia dryer, and an ammonia liquefier, which are connected in this order; the hydrogen iodide generator is also respectively connected with a phosphorus pentoxide storage tank and a phosphoric acid storage tank; the gas-solid separator is also connected with a condensation separator, and the condensation separator is respectively connected with the plasma reactor and the elemental iodine storage tank; the device also comprises an air separator, wherein the air separator is respectively connected with a nitrogen storage tank and an oxygen storage tank, the nitrogen storage tank is connected with the plasma reactor, the oxygen storage tank is connected with a tin dioxide regenerator, and the tin dioxide regenerator is also connected with an elemental iodine storage tank and a bunsen reaction tower in sequence. The liquefied ammonia can be stored in an ammonia storage tank, so that long-distance transportation is realized, and after the ammonia is transported to a destination, the ammonia is sent to an ammonia decomposer to be decomposed into hydrogen and nitrogen, and finally, the preparation of the hydrogen is realized.
Referring to fig. 1 and 2, the ammonia-based hydrogen production system of the present application operates as follows: after the system is stable, (1) the Bunsen reaction, SO in the Bunsen reaction tower 2 、I 2 React with water to generate H 2 SO 4 And HI, and layering the mixed acid aqueous solution to obtain 40-57 wt% of hydroiodic acid aqueous solution. (2) And (3) preparing hydrogen iodide gas, namely sending the 40-57 wt% aqueous solution of hydrogen iodide obtained by the separation of the bunsen reaction into a hydrogen iodide gas generator, and simultaneously, dehydrating agent phosphorus pentoxide absorbs water in the aqueous solution of hydrogen iodide and emits a large amount of heat, wherein the hydrogen iodide gas generator can circulate through cooling water to keep the internal temperature of the hydrogen iodide gas generator to be lower than 573K, and the hydrogen iodide gas is generated due to the loss of water. (3) The plasma reaction prepares ammonium iodide, hydrogen iodide gas is taken as raw material to enter a plasma reactor, and nitrogen in a nitrogen storage tank is also introduced into the plasma reactor. In the plasma reactor, the frequency of dielectric barrier discharge is 1 kHz-12 kHz, the input voltage is 1 kV-40 kV, the molar ratio of nitrogen and hydrogen iodide gas in the plasma reactor is controlled to be 1:6-20, the temperature is controlled to be 458K-573K, the pressure is controlled to be 0.1 MPa-10 MPa, and the reaction time is controlled to be 10 min-120 min. Reverse-rotationAfter that, the mixed gas a in the plasma reactor contains ammonium iodide particles, iodine vapor, hydrogen iodide gas, and nitrogen gas. (4) And (3) carrying out gas-solid separation, wherein the mixed gas A is sent to a gas-solid separator, in the gas-solid separator, ammonium iodide particles in the mixed gas A are agglomerated and separated, at the moment, the temperature in the gas-solid separator is controlled to be higher than 458K, the separated ammonium iodide solid is sent to an ammonium iodide decomposer, and the rest of mixed gas B containing iodine vapor, hydrogen iodide and nitrogen is sent to a condensation separator. After entering a condensation separator, the mixed gas B is cooled down to 293K-313K, iodine vapor in the mixed gas is sublimated and separated out, iodine solid is collected into an elemental iodine storage tank, and the residual mixed gas C containing hydrogen iodide gas and nitrogen is returned to a plasma reactor for continuous reaction. (5) And (3) decomposing ammonium iodide and reacting tin iodide, wherein in an ammonium iodide decomposer, a gas-solid separator separates the obtained ammonium iodide solid and tin dioxide solid, the mixture is heated to 673-723K, the decomposition time is controlled to be 10-60 min, during which the ammonium iodide is decomposed into ammonia gas and hydrogen iodide, and the hydrogen iodide reacts with the tin dioxide in the reactor to generate tin tetraiodide and water. (6) After the ammonia storage and transportation and tin-iodine reaction are finished, the mixed gas D containing ammonia, tetraiodide and water is sent into a tin dioxide regenerator, the mixed gas D is cooled to 473K-623K, the tetraiodide tin gas is liquefied, the rest mixed gas containing ammonia and steam is sent into an ammonia dryer, then oxygen generated by an air separator is sent into the tin dioxide regenerator, the temperature is raised to 673K-773K, the tetraiodide tin reacts with the oxygen to generate tin dioxide solid particles and iodine steam, the tin dioxide solid particles are recycled into an ammonium iodide decomposer for recycling, the iodine steam is cooled and sublimated into solid to be stored in an elemental iodine storage tank, and iodine solid in the iodine storage tank returns to be recycled to participate in the autogenous reaction. The ammonia gas dryer is filled with calcium oxide powder, and then the dried ammonia gas is liquefied into liquid ammonia in an ammonia gas storage tank by a cooling or pressurizing mode in the ammonia gas liquefier for storage. (7) And (3) decomposing ammonia to prepare hydrogen, and decomposing ammonia to generate nitrogen and hydrogen after transporting the liquid ammonia to a destination.
The principles to which this application relates are: and (one) preparing ammonium iodide by plasma reaction. Plasma (PDP)The body has unique physical and chemical properties, and can weaken and even eliminate the limit of thermodynamics on the synthetic ammonia reaction, so that the synthetic ammonia reaction can be carried out under relatively mild conditions. By using low temperature plasma technology such as corona discharge, thomson discharge, dielectric barrier discharge, etc., preferably dielectric barrier discharge, the reaction gas nitrogen and hydrogen iodide will be ionized and activated into N, H, I, etc., radicals which then form ammonia and iodine elementary substance under the action of a catalyst mainly composed of a metal carrier and a carrier, the metal carrier comprises one or more of Ni, fe, co, cu, ru, mo, etc., the carrier comprises Al 2 O 3 、SiO 2 、TiO 2 One of MgO, AC, etc. The reaction equations involved include: n (N) 2 +6HI →2NH 3 +3I 2 ；NH 3 +HI →NH 4 I。
And (II) decomposing ammonium iodide to prepare ammonia gas. Ammonium iodide is a white crystal of the formula NH 4 I, ammonium iodide is a relatively stable substance under normal temperature and pressure, but when it is heated to 673K to 723K, the ammonium iodide undergoes thermal decomposition, and the decomposition reaction is divided into two steps: (1) Thermal decomposition of ammonium iodide to ammonia gas and hydrogen iodide NH 4 I →NH 3 +HI; (2) Partial decomposition of Hydrogen iodide into Hydrogen and iodine vapor 2HI ↔ H 2 +I 2 . However, if a catalyst is not used, the decomposition rate of ammonium iodide at 673K to 723K may be close to 100%, but the decomposition rate of hydrogen iodide is lower than 1%, which is almost negligible. At the same time, once the temperature of the gas is reduced, ammonia gas and hydrogen iodide can rapidly react to generate ammonium iodide solid small particles. So to obtain ammonia, in situ separation of ammonia or hydrogen iodide must be achieved under high temperature conditions (e.g., 673K-723K).
There are two ideas here: (1) directly adsorbing and separating ammonia; (2) adsorption separation of hydrogen iodide or consumption of hydrogen iodide. Japanese patent JP5660493B2 mentions that ammonia can be adsorbed using USY zeolite to achieve in situ separation. However, the strong corrosiveness of hydrogen iodide at high temperature greatly reduces the service life of the zeolite for ammonia separation. In addition, assuming that the USY zeolite or a modified USY zeolite can absorb ammonia generated by thermal decomposition of ammonium iodide at 673K-723K, the USY zeolite absorbing ammonia may need a higher temperature to desorb ammonia, and the temperature higher than 723K can completely accelerate the decomposition of ammonia itself, thereby reducing the ammonia production efficiency of the system.
In view of in-situ consumption of hydrogen iodide, the application provides a method for recycling tin element to consume hydrogen iodide so as to separate ammonia generated by thermal decomposition of ammonium iodide and further prepare ammonia. Specifically, tin dioxide and ammonium iodide are mixed and heated to 673K-773K, ammonia gas and hydrogen iodide are generated by thermal decomposition of the ammonium iodide, and at the moment, the hydrogen iodide reacts with the tin dioxide to generate tetratin iodide and water. The chemical reactions involved are: NH (NH) 4 I →NH 3 +HI；4HI +SnO 2 →SnI 4 +2H 2 O, total reaction is 4NH 4 I +SnO 2 →4NH 3 +SnI 4 +2H 2 O. After the reaction, the temperature of the mixed gas is reduced to below 637K, for example, to 573K-637K, and the tin tetraiodide is converted into liquid from gas, but at the moment, ammonia and water are still gas, and the ammonia mixed with water vapor can be obtained after gas-liquid separation.
After separating ammonia and water, controlling the reaction temperature between 623K and 723K, and oxidizing tin tetraiodide by using oxygen obtained by air separation to generate tin dioxide and elemental iodine. At the moment, the tin dioxide is solid, the elemental iodine is gas, and the tin dioxide powder is recovered through gas-solid separation for recycling. The chemical reaction formula is as follows: snI (SnI) 4 +O 2 →SnO 2 +I 2 。
Through the above process, the ammonium iodide is converted into ammonia gas with water vapor and elemental iodine through two steps. The ammonia with water vapor can be dried by using calcium oxide, and the dried ammonia can be converted into liquid ammonia by means of cooling or pressurizing. Meanwhile, the elemental iodine can be returned to the bunsen reaction system for recycling.
The nitrogen produced by the air separation equipment and the hydrogen iodide produced by the bunsen reaction system are used as raw materials for preparing ammonia. Compared with the plasma ammonia synthesis technology using nitrogen and hydrogen as raw materials, the method has the following advantages: the dissociation energy of the iodized hydrogen is 299kJ/mol, which is lower than that of the hydrogen, and the energy consumption for synthesizing ammonia is lower. In the reaction, the hydrogen iodide is excessive, and ammonia gas generated by the reaction can react with the hydrogen iodide rapidly to generate ammonium iodide solid. Ammonium iodide can exist stably as long as the voltage and the discharge frequency are controlled, so that ammonia gas is not ionized and decomposed. The hydrogen iodide gas serving as a hydrogen source can be regenerated through the bunsen reaction system, and carbon dioxide is not generated in the regeneration process of the hydrogen iodide after the bunsen reaction system is matched with green heat sources such as nuclear energy, solar energy and the like.
And (III) decomposing and utilizing ammonia gas. In the ammonia decomposer, the liquid ammonia is heated and gasified to 673K-873K, and the ammonia is decomposed to form nitrogen and hydrogen under the catalysis of the ammonia decomposition catalyst. Then, pressure swing adsorption principle PSA is adopted to separate nitrogen and hydrogen at normal temperature.
Example 1
The reaction solution of the Bunsen reaction column was layered to obtain 1000g of a 40wt% aqueous hydrogen iodide solution, which was contacted with phosphorus pentoxide in a hydrogen iodide generator, and about 399.36g of hydrogen iodide gas was produced and fed into a plasma reactor. At this time, 14.56g of nitrogen gas was also fed into the plasma reactor. In the plasma reactor, the reaction temperature was controlled at 473K and the reaction pressure was controlled at 1.75MPa. The reactor was filled with 100g of Co-Ni/Al 2 O 3 The input voltage of the catalyst and the dielectric barrier discharge device is 14.8kV, and the frequency is 8.5kHz. After the reaction was carried out for 60 minutes, about 19% nitrogen was converted to give 28.71g of ammonium iodide. The remaining unconverted nitrogen, hydrogen iodide gas and iodine vapor, the ammonium iodide particles enter a gas-solid separator, the temperature is controlled at 473K, and the ammonium iodide particles are separated into an ammonium iodide decomposer. The gas temperature was reduced to 313k,75.43g of iodine solids were separated, and the remaining nitrogen and hydrogen iodide gas were returned to the plasma reactor. In an ammonium iodide decomposer, 28.71g of ammonium iodide was mixed with an excess of tin dioxide powder, and the mixture was heated to 723K, after 20 minutes of reaction, 3.36g of ammonia gas and 31.02g of tin iodide and water vapor were produced. The above-mentioned product is fed into tin dioxide regenerator, and the mixtureFirstly, cooling to 573K, liquefying tin iodide, separating out, and collecting and storing ammonia gas with water vapor as a system product. The temperature in the tin dioxide regenerator was then raised to 723K and excess oxygen was added and the tin iodide reacted with oxygen to produce 25.14g of tin dioxide and 7.46g of elemental iodine. The tin dioxide returns to the ammonium iodide decomposer, and the iodine simple substance is stored in the simple substance iodine storage tank.
Example 2
The reaction solution of the Bunsen reaction column was layered to obtain 1280g of a 50wt% aqueous hydrogen iodide solution, which was contacted with phosphorus pentoxide in a hydrogen iodide generator, and about 607.03g of hydrogen iodide gas was produced and fed into a plasma reactor. At this time, 22.13g of nitrogen gas was also fed into the plasma reactor. In the plasma reactor, the reaction temperature was controlled at 503K and the reaction pressure was controlled at 1.89MPa. The reactor was filled with 200g of Co-Ni/Al 2 O 3 The input voltage of the catalyst and the dielectric barrier discharge device is 19.8kV, and the frequency is 8.5kHz. After 75min of reaction, about 18% nitrogen shift, 43.64g of ammonium iodide was obtained. The remaining unconverted nitrogen, hydrogen iodide gas and iodine vapor, the ammonium iodide particles enter a gas-solid separator, the temperature is controlled at 473K, and the ammonium iodide particles are separated into an ammonium iodide decomposer. The gas temperature was reduced to 313k,114.65g of iodine solids were separated, and the remaining nitrogen and hydrogen iodide gas were returned to the plasma reactor. In an ammonium iodide decomposer, 43.64g of ammonium iodide was mixed with an excess of tin dioxide powder, and the mixture was heated to 723K, and after 30 minutes of reaction, 5.10g of ammonia gas and 47.15g of tin iodide and water vapor were produced. The above-mentioned products enter into tin dioxide regenerator, the mixture is cooled to 573K first, tin iodide is liquefied and separated out, ammonia gas with water vapor is collected and stored as system product. The temperature in the tin dioxide regenerator was then raised to 723K and excess oxygen was added and the tin iodide reacted with oxygen to produce 38.21g of tin dioxide and 11.34g of elemental iodine. The tin dioxide returns to the ammonium iodide decomposer, and the iodine simple substance is stored in the simple substance iodine storage tank.
While embodiments of the present application have been illustrated and described above, it will be appreciated that the above-described embodiments are exemplary and should not be construed as limiting the present application. Various changes and modifications may be made to the present application without departing from the spirit and scope of the application, and such changes and modifications fall within the scope of the application as hereinafter claimed.
Claims (10)
1. The ammonia-based hydrogen production method comprises the steps of S1 Bunsen reaction, and layering a Bunsen reaction solution to obtain a hydroiodic acid aqueous solution, and is characterized in that: s2, preparing hydrogen iodide gas, namely mixing a hydroiodic acid water solution with phosphorus pentoxide to obtain the hydrogen iodide gas;
s3, performing plasma reaction to prepare ammonium iodide, and reacting nitrogen with hydrogen iodide gas of S2 by using a low-temperature plasma technology to obtain mixed gas A;
s4, gas-solid separation, wherein the temperature of the mixed gas A of S3 is kept higher than 458K, and the ammonium iodide solid is obtained through the first gas-solid separation; or the temperature of the mixed gas A in the step S3 is kept higher than 458K, ammonium iodide solid is obtained through the first gas-solid separation, the temperature of the residual mixed gas B in the first gas-solid separation is reduced to 293K-313K, the obtained elemental iodine is sent to an elemental iodine storage tank through the second gas-solid separation, and the residual mixed gas C is returned to the step S3 for continuous plasma reaction;
s5, decomposing ammonium iodide and reacting tin iodine, mixing and heating the ammonium iodide solid obtained by S4 and the tin dioxide solid, and reacting hydrogen iodide generated by decomposing the ammonium iodide with the tin dioxide to obtain a mixed gas D;
s6, ammonia storage and transportation, wherein the mixed gas D in S5 is cooled to 473K-623K, the tin tetraiodide gas is liquefied and separated, and the rest mixed gas is cooled or pressurized and liquefied into liquid ammonia after being dried;
s7, decomposing ammonia to prepare hydrogen, and decomposing ammonia to prepare hydrogen after transporting the liquid ammonia to a destination.
2. A method for producing hydrogen based on ammonia as defined in claim 1, wherein: layering the Bunsen reaction solution of S1 to obtain 40-57 wt% aqueous solution of hydroiodic acid, and mixing the aqueous solution of hydroiodic acid with phosphorus pentoxide by sending the aqueous solution of hydroiodic acid into S2, wherein the temperature of the mixed solution is controlled to be lower than 573K.
3. A method for producing hydrogen based on ammonia as defined in claim 1, wherein: the molar ratio of the nitrogen to the hydrogen iodide gas in the S3 is 1:6-20, the reaction temperature is 458K-573K, the reaction pressure is 0.1 MPa-10 MPa, and the reaction time is 10 min-120 min.
4. A method for producing hydrogen based on ammonia as defined in claim 1, wherein: the low-temperature plasma technology is selected from corona discharge, thomson discharge and dielectric barrier discharge, and when the low-temperature plasma technology selects the dielectric barrier discharge, the frequency of the dielectric barrier discharge is 1 kHz-12 kHz, and the input voltage is 1 kV-40 kV.
5. A method for producing hydrogen based on ammonia as defined in claim 1, wherein: and in the step S5, the ammonium iodide solid and the tin dioxide solid are mixed, the mixture is heated to 673K-723K, and the decomposition time is 10 min-60 min.
6. A method for producing hydrogen based on ammonia as defined in claim 1, wherein: and in the step S6, calcium oxide is adopted for drying.
7. A method for producing hydrogen based on ammonia as defined in claim 1, wherein: the method also comprises the regeneration of tin dioxide, wherein the tin tetraiodide separated in the S6 reacts with oxygen under the condition of 673K-773K to generate tin dioxide solid particles and iodine vapor, the recovered tin dioxide solid particles are returned to the S5 to continuously participate in tin-iodine reaction, and the iodine vapor is cooled and sublimated into solid which is returned to the S1 to participate in the Bunsen reaction.
8. A method for producing hydrogen based on ammonia as defined in claim 7, wherein: the nitrogen required for the S3 and/or the oxygen required for the regeneration of the tin dioxide are prepared by an air separator.
9. An ammonia-based hydrogen production system operating in accordance with the method of claim 1, wherein: comprises a Bunsen reaction tower, a two-phase layering device, a hydrogen iodide generator, a plasma reactor, a gas-solid separator, an ammonium iodide decomposer, a tin dioxide regenerator, an ammonia dryer and an ammonia liquefier which are connected in sequence; the hydrogen iodide generator is also respectively connected with a phosphorus pentoxide storage tank and a phosphoric acid storage tank; the gas-solid separator is also connected with a condensation separator, and the condensation separator is respectively connected with the plasma reactor and the elemental iodine storage tank; the tin dioxide regenerator is also connected with the elemental iodine storage tank and the bunsen reaction tower in sequence, liquefied ammonia is stored in the ammonia storage tank, so that long-distance transportation is realized, and after the ammonia is transported to a destination, the ammonia is sent into the ammonia decomposer to be decomposed into hydrogen and nitrogen, and finally the preparation of the hydrogen is realized.
10. An ammonia-based hydrogen production system as defined in claim 9, wherein: the device also comprises an air separator, wherein the air separator is respectively connected with a nitrogen storage tank and an oxygen storage tank, the nitrogen storage tank is connected with the plasma reactor, and the oxygen storage tank is connected with the tin dioxide regenerator.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1442950A (en) * | 1973-12-12 | 1976-07-14 | Euratom | Process for the production of hydrogen |
| JP2000247658A (en) * | 1999-02-23 | 2000-09-12 | Asahi Glass Co Ltd | Production of float glass |
| CN101618292A (en) * | 2008-11-10 | 2010-01-06 | 李元胜 | System for comprehensive utilization of three industrial wastes |
| JP2020083716A (en) * | 2018-11-28 | 2020-06-04 | 株式会社エスイー | Material production method for production of hydrogen generating material containing magnesium hydride with improved formation reaction of magnesium hydride, and, hydrogen production method using hydrogen generating material containing magnesium hydride produced by the material production method |
| CN113167504A (en) * | 2018-12-11 | 2021-07-23 | 绿净星球股份有限公司 | Heat utilization system and heat generating device |
| EP3896364A1 (en) * | 2018-12-11 | 2021-10-20 | Clean Planet Inc. | Heat utilization system, and heat generating device |
| CN116715191A (en) * | 2023-08-08 | 2023-09-08 | 浙江百能科技有限公司 | Sulfuric acid phase decomposition process and system for cyclic hydrogen production by sulfur and iodine |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2010331314A1 (en) * | 2009-12-14 | 2012-06-28 | Nippon Shokubai Co., Ltd. | Process for synthesis of ammonia |
-
2023
- 2023-11-02 CN CN202311444122.5A patent/CN117163919B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1442950A (en) * | 1973-12-12 | 1976-07-14 | Euratom | Process for the production of hydrogen |
| JP2000247658A (en) * | 1999-02-23 | 2000-09-12 | Asahi Glass Co Ltd | Production of float glass |
| CN101618292A (en) * | 2008-11-10 | 2010-01-06 | 李元胜 | System for comprehensive utilization of three industrial wastes |
| JP2020083716A (en) * | 2018-11-28 | 2020-06-04 | 株式会社エスイー | Material production method for production of hydrogen generating material containing magnesium hydride with improved formation reaction of magnesium hydride, and, hydrogen production method using hydrogen generating material containing magnesium hydride produced by the material production method |
| CN113167504A (en) * | 2018-12-11 | 2021-07-23 | 绿净星球股份有限公司 | Heat utilization system and heat generating device |
| EP3896364A1 (en) * | 2018-12-11 | 2021-10-20 | Clean Planet Inc. | Heat utilization system, and heat generating device |
| CN116715191A (en) * | 2023-08-08 | 2023-09-08 | 浙江百能科技有限公司 | Sulfuric acid phase decomposition process and system for cyclic hydrogen production by sulfur and iodine |
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