CN207418314U - The system for recycling carbon dioxide - Google Patents
The system for recycling carbon dioxide Download PDFInfo
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- CN207418314U CN207418314U CN201721474838.XU CN201721474838U CN207418314U CN 207418314 U CN207418314 U CN 207418314U CN 201721474838 U CN201721474838 U CN 201721474838U CN 207418314 U CN207418314 U CN 207418314U
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- reactor
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- carbonation
- calcium
- carbon dioxide
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 172
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 82
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 82
- 238000004064 recycling Methods 0.000 title claims abstract description 58
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims abstract description 130
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims abstract description 89
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 88
- 238000006243 chemical reaction Methods 0.000 claims abstract description 73
- 235000019270 ammonium chloride Nutrition 0.000 claims abstract description 65
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims abstract description 45
- 229910000019 calcium carbonate Inorganic materials 0.000 claims abstract description 45
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims abstract description 44
- 235000012241 calcium silicate Nutrition 0.000 claims abstract description 41
- 239000001110 calcium chloride Substances 0.000 claims abstract description 35
- 229910001628 calcium chloride Inorganic materials 0.000 claims abstract description 35
- 239000000378 calcium silicate Substances 0.000 claims abstract description 31
- 229910052918 calcium silicate Inorganic materials 0.000 claims abstract description 31
- HCWCAKKEBCNQJP-UHFFFAOYSA-N magnesium orthosilicate Chemical compound [Mg+2].[Mg+2].[O-][Si]([O-])([O-])[O-] HCWCAKKEBCNQJP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000000391 magnesium silicate Substances 0.000 claims abstract description 31
- 229910052919 magnesium silicate Inorganic materials 0.000 claims abstract description 31
- 235000019792 magnesium silicate Nutrition 0.000 claims abstract description 31
- 229960003340 calcium silicate Drugs 0.000 claims abstract description 28
- OYACROKNLOSFPA-UHFFFAOYSA-N calcium;dioxido(oxo)silane Chemical compound [Ca+2].[O-][Si]([O-])=O OYACROKNLOSFPA-UHFFFAOYSA-N 0.000 claims abstract description 28
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims abstract description 25
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000001095 magnesium carbonate Substances 0.000 claims abstract description 24
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims abstract description 24
- 229910001629 magnesium chloride Inorganic materials 0.000 claims abstract description 22
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 19
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 19
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000000908 ammonium hydroxide Substances 0.000 claims abstract description 17
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 95
- 229960004424 carbon dioxide Drugs 0.000 claims description 70
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 68
- 239000000243 solution Substances 0.000 claims description 47
- 229910021529 ammonia Inorganic materials 0.000 claims description 42
- 239000000377 silicon dioxide Substances 0.000 claims description 29
- 230000008859 change Effects 0.000 claims description 14
- 238000001704 evaporation Methods 0.000 claims description 12
- 230000008929 regeneration Effects 0.000 claims description 12
- 238000011069 regeneration method Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 9
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 6
- 229910002090 carbon oxide Inorganic materials 0.000 claims description 6
- 239000000460 chlorine Substances 0.000 claims description 6
- 229910052801 chlorine Inorganic materials 0.000 claims description 6
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 4
- 150000003863 ammonium salts Chemical class 0.000 claims description 4
- 239000011777 magnesium Substances 0.000 claims description 4
- 229910052749 magnesium Inorganic materials 0.000 claims description 4
- 239000012266 salt solution Substances 0.000 claims description 4
- 238000004062 sedimentation Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 claims 1
- 229910052739 hydrogen Inorganic materials 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 47
- 239000003054 catalyst Substances 0.000 abstract description 21
- 238000005265 energy consumption Methods 0.000 abstract description 14
- 235000010216 calcium carbonate Nutrition 0.000 description 35
- 230000008569 process Effects 0.000 description 27
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 19
- 239000007787 solid Substances 0.000 description 18
- 229910052681 coesite Inorganic materials 0.000 description 12
- 229910052906 cristobalite Inorganic materials 0.000 description 12
- 239000002245 particle Substances 0.000 description 12
- 229910052682 stishovite Inorganic materials 0.000 description 12
- 229910052905 tridymite Inorganic materials 0.000 description 12
- 239000000725 suspension Substances 0.000 description 10
- 239000008187 granular material Substances 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 229910052799 carbon Inorganic materials 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 8
- XNEYCQMMVLAXTN-UHFFFAOYSA-N carbonic acid;magnesium Chemical compound [Mg].OC(O)=O XNEYCQMMVLAXTN-UHFFFAOYSA-N 0.000 description 7
- 239000007791 liquid phase Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 7
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 5
- 229910052500 inorganic mineral Inorganic materials 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000011707 mineral Substances 0.000 description 5
- 235000010755 mineral Nutrition 0.000 description 5
- 238000005201 scrubbing Methods 0.000 description 5
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 5
- 235000012239 silicon dioxide Nutrition 0.000 description 5
- 230000001351 cycling effect Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000010419 fine particle Substances 0.000 description 4
- 230000002045 lasting effect Effects 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 230000009919 sequestration Effects 0.000 description 4
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 3
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 159000000003 magnesium salts Chemical class 0.000 description 3
- 230000020477 pH reduction Effects 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 229910052710 silicon Inorganic materials 0.000 description 3
- 239000010703 silicon Substances 0.000 description 3
- 159000000000 sodium salts Chemical class 0.000 description 3
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- 239000004566 building material Substances 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000008247 solid mixture Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- JHXCINJSAAFBDH-UHFFFAOYSA-N [Ca].O[Si](O)(O)O Chemical compound [Ca].O[Si](O)(O)O JHXCINJSAAFBDH-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910021386 carbon form Inorganic materials 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 230000009719 regenerative response Effects 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- PANBYUAFMMOFOV-UHFFFAOYSA-N sodium;sulfuric acid Chemical compound [Na].OS(O)(=O)=O PANBYUAFMMOFOV-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- FKHIFSZMMVMEQY-UHFFFAOYSA-N talc Chemical compound [Mg+2].[O-][Si]([O-])=O FKHIFSZMMVMEQY-UHFFFAOYSA-N 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The utility model discloses it is a kind of recycle carbon dioxide system, including：Chlorination reactor for that will contain calcium-silicate and/or chlorination containing magnesium silicate, obtains calcium chloride and/or magnesium chloride；Carbonation reactor is connected with chlorination reactor, for by calcium chloride and/or magnesium chloride and ammonium hydroxide and carbon dioxide mix and carrying out carbonation reaction, as calcium carbonate and/or magnesium carbonate, while carbon dioxide conversion is generated ammonium chloride solution；And retracting device, it is connected between carbonation reactor and chlorination reactor, for recycling the ammonium chloride solution of carbonation reactor generation, is fed directly to after decomposition reaction generates hydrogen chloride or concentration in chlorination reactor.The utility model uses the purity height of catalyst of the ammonium chloride as entire carbon dioxide mineralising reaction, final products calcium carbonate and/or magnesium carbonate, and low energy consumption；Technique realizes the recycling of ammonium chloride, reduces supplies consumption compared with prior art.
Description
Technical field
The utility model is related to chemical industry and field of Environment Protection, relate more specifically to a kind of system for recycling carbon dioxide.
Background technology
It collects and recycles carbon dioxide, be reply climate change to reduce greenhouse gas emission, environment and ecology are led
The technical issues of important in domain.At present, the collection disposal of carbon dioxide mainly includes geological reservoir, Ocean storage, mineralize storage
Deposit with biological sequestration etc..The mineral carbonation fixation of carbon dioxide refers to carbon dioxide with containing alkalescence or alkaline earth oxide
Ore (mainly the ore of calcium and magnesium silicate or the discarded object of industry and building materials) reaction, generation carbonate is so as to being mothballed
A series of processes.The storage that mineralizes is the absorption process of carbon dioxide in nature, and the carbonate generated is the heat of carbon
Mechanics stable form, and have no effect to environment, therefore the fixation that is carbonated is a kind of most stable and safest carbon sequestration mode.
Therefore, mineral carbonation carbon sequestration is the best selection of carbon dioxide collection disposal technology.However, mineral carbonation carbon-fixation-technology,
Not yet realize industrial applications at present, existing technical solution, there is such as reaction rate is slow, high energy consumption is of high cost,
The problems such as Technical Economy is poor.
At present, the carbonating technique for fixing and technology of the carbon dioxide of open report, is carbonated including direct dry method gas-solid
It is carbonated with liquid phase scrubbing.Using carbon dioxide the generation of one step gas-solid reaction directly occurs with ore for direct dry method gas-solid carbonating
The route of carbonate.The reaction scheme reaction rate is slow, and efficiency is low, even if pressurizeing to improve reaction rate, it is also difficult to meet big
The needs that technical scale absorbs.Therefore, liquid phase scrubbing carbonating becomes main carbonating carbon-fixation-technology.
Liquid phase scrubbing carbonating can be divided into direct absorption process and indirect absorption process again.Direct absorption process is by calcium and magnesium silicate
It waits after ores are ground into fine particle, generates carbonate with carbon dioxide reaction in the liquid phase, essential reaction and directly do
Method gas-solid carbonating be not different, only because in the liquid phase carbon dioxide solubility be carbonic acid, further with tiny ore
During grain reaction, the rate of reaction is greatly improved.The grinding cost of ore is very high, and reaction rate cannot still meet greatly
The needs that scale absorbs, therefore the method is not still best selection in economy and high efficiency.Indirect liquid phase scrubbing rule will
Ore first converts to obtain alkaline solution or suspension (hereinafter referred to as lye), and absorbing carbon dioxide and forms carbonic acid in lye
Salt further separates carbonate with sequestration of carbon dioxide.Two core links of the method are conversion and the carbon dioxide of ore
It absorbs.It is different that the route of alkaline solution is obtained according to used minerals and its conversion, different process routes can be obtained；
And it is different (solution, suspension or emulsion) according to the system of absorbing reaction, absorbing reaction also has different technical solutions.
Since sodium salt is widely present, cheap, and sodium hydroxide has very high solubility in water, therefore with sodium salt
Technique to absorb minerals is suggested and realizes industrialization first.Typical technique is usually by being electrolysed sodium salt (such as sulfuric acid
Sodium) sodium hydroxide is obtained, with sodium hydroxide absorbing carbon dioxide, obtain sodium acid carbonate or sodium carbonate.But the technology is because using
The electrolysis of high energy consumption obtains sodium hydroxide and it is made to lose competitiveness in economy.Because the solubility of sodium hydroxide in water
Height, therefore its absorption process is the neutralization reaction in solution, reaction rate is fast, and the design of reactor is also by a relatively simple.
Existing indirect liquid phase scrubbing method such as CN104284707A disclose it is a kind of using calcium-silicate, with hydrogen chloride matchmaker
It is situated between, using magnesium salts as the indirect routes of hydroxyl carrier.The technological deficiency that the technology path is primarily present is：In order to realize magnesium chloride
Recycling, which needs magnesium chloride being heated to high temperature (450 DEG C or more), generates magnesia or alkali formula chlorination
Magnesium so that whole process energy consumption is higher.
Utility model content
In view of this, it is higher the purpose of this utility model is to provide a kind of reaction rate and energy consumption and cost are lower
The system for recycling carbon dioxide.
The utility model provides a kind of system for recycling carbon dioxide, including：Chlorination reactor, for by calcic silicon
Hydrochlorate and/or chlorination containing magnesium silicate obtain calcium chloride and/or magnesium chloride；Carbonation reactor connects with the chlorination reactor
Connect, for by the calcium chloride and/or magnesium chloride and ammonium hydroxide and carbon dioxide mix and carrying out carbonation reaction, will described in
Carbon dioxide conversion is calcium carbonate and/or magnesium carbonate, while generates ammonium chloride solution；And retracting device, it is connected to the carbon
Between acidification reactor and the chlorination reactor, for recycling the ammonium chloride solution that the carbonation reactor generates,
It is fed directly to after decomposition reaction generates hydrogen chloride or concentration in the chlorination reactor.
Preferably, silica is also generated in the chlorination reactor, the system also includes：First separator, connection
Between the chlorination reactor and the carbonation reactor, for will be discharged after silica separation.
Preferably, the calcium carbonate and/or magnesium carbonate in the carbonation reactor after sedimentation separation by discharging.
Preferably, the system also includes：Second separator is connected to the carbonation reactor and the retracting device
Between, for will be discharged after calcium carbonate and/or magnesium carbonate separation.
It preferably, will be described containing calcium-silicate and/or anti-with ammonium chloride containing magnesium silicate in the chlorination reactor
Should, also generate ammonia in the chlorination reactor.
Preferably, ammonia pipeline is also set up between the chlorination reactor and the carbonation reactor, by the chlorine
Change the ammonia that reactor generates to send into the carbonation reactor.
Preferably, the retracting device is evaporation concentrator, and the evaporation concentrator is by the ammonium chloride solution of recycling
Vapor and the ammonium chloride solution of concentration are separated into, wherein the ammonium chloride solution concentrated is sent to the chlorination reaction
Device.
Preferably, the evaporation concentrator is also connected by heat exchanger with first separator.
It preferably, will be described containing calcium-silicate and/or anti-with ammonium chloride containing magnesium silicate in the chlorination reactor
It should.
Preferably, the retracting device is ammonia regeneration reactor, and the ammonia regeneration reactor is by the chlorine of recycling
Change ammonium salt solution and be decomposed into ammonia and hydrogen chloride, wherein the hydrogen chloride decomposed is sent to the chlorination reactor.
Preferably, the ammonia regeneration reactor is also connected by gas piping with the carbonation reactor, for inciting somebody to action
The obtained ammonia is decomposed to send to the carbonation reactor.
Preferably, the chlorination reactor is one of stirred tank, rotary furnace.
Preferably, the carbonation reactor is one of bubble tower, Airlift circulating reactor, fluid bed.
The system according to the present utility model for recycling carbon dioxide, using ammonium chloride as entire carbon dioxide mineralising
The catalyst of reaction, and the recycling of ammonium chloride is realized, entire technical process reduces material and disappears compared with prior art
Consumption.
The recycling of catalyst ammonium chloride in the utility model can be realized under conditions of middle low temperature, with existing skill
Art compares for example with technical solution of the magnesium chloride as catalyst, need not catalyst be heated to high temperature and recycled,
Significantly reduce the energy consumption of process.
Description of the drawings
By the description referring to the drawings to the utility model embodiment, above-mentioned and other mesh of the utility model
, feature and advantage will be apparent from.
Fig. 1 shows the flow chart of the method for the recycling carbon dioxide according to the utility model first embodiment；
Fig. 2 shows the flow chart of the method for the recycling carbon dioxide according to the utility model second embodiment；
Fig. 3 shows the structure diagram of the system of the recycling carbon dioxide according to the utility model first embodiment；
Fig. 4 shows the structure diagram of the system of the recycling carbon dioxide according to the utility model second embodiment.
Specific embodiment
Hereinafter reference will be made to the drawings is more fully described the utility model.In various figures, identical element is using similar
Reference numeral represent.For the sake of clarity, the various pieces in attached drawing are not necessarily to scale.It in addition, may in figure
Some well known parts are not shown.
Many specific details of the utility model, such as the structure of component, material, size, place is described hereinafter
Science and engineering skill and technology, to be more clearly understood that the utility model.But just as the skilled person will understand,
The utility model can not be realized according to these specific details.
The utility model provides a kind of recycling carbon dioxide (CO2) system, it is huge and honest and clean using reserves
Valency contains calcium-silicate and/or absorbing carbon dioxide containing magnesium silicate, and ultimately generates the calcium carbonate (CaCO of solid state3)、
Magnesium carbonate (MgCO3) etc. carbonate.Calcium carbonate or magnesium carbonate are widely used in industrial quarters, and carbon dioxide can be well realized
It recycles.
It can be the silicate of any calcic and/or magnesium ion containing calcium-silicate and/or containing magnesium silicate, be, for example, silicic acid
Calcium (CaSiO3), magnesium silicate (MgSiO3) and the two arbitrary proportion mixture, source can be silicate ore, contain
The trade waste of calcium/magnesium silicate or the discarded concrete of building trade, discarded building materials etc..In the utility model, with calcic
Silicate and/or containing magnesium silicate illustrated exemplified by calcium silicates, using other containing calcium-silicate and/or containing magnesium silicate
Recycling carbon dioxide system principle it is similar therewith.
Carbon dioxide can be that include flue gas etc. various with carbon dioxide and air gas as main component, wherein two
The volume content of carbonoxide is 0.05%~99.95%.
Fig. 1 shows the flow chart of the method for the recycling carbon dioxide according to the utility model first embodiment, including
Step S101 to step S105.
In step S101, chlorination is carried out, calcium-silicate and/or chlorination containing magnesium silicate will be contained, obtain calcium chloride
(CaCl2) and/or magnesium chloride (MgCl2).In the present embodiment, chlorinating step includes that described calcium-silicate and/or silicic acid containing magnesium will be contained
Salt is reacted with ammonium chloride, in this step in addition to calcium chloride is generated, also generates silica (SiO2) and ammonia (NH3).It is specific anti-
Process is answered to be shown below (exemplified by containing calcium-silicate and/or be calcium silicates containing magnesium silicate)：
CaSiO3+NH4Cl→CaCl2+SiO2↓+NH3↑
Calcium silicates can be particle, ammonium chloride can be solid powder or concentration for 1% to saturated concentration it is molten
Liquid, reaction temperature can be at 80 DEG C to 600 DEG C.
In step s 102, first time separation is carried out, is discharged after the silica generated in step S101 is separated.Specifically
Ground, what is obtained after can step S101 be reacted is passed through first with the suspension that silica dioxide granule forms by calcium chloride solution and separates
In device, interior temperature can be controlled at 25 DEG C to 400 DEG C, and silica dioxide granule is discharged after separator bottom sedimentation, through into one
Fine silica particle is generated after step is dry, becomes first final products.
In step s 103, it is carbonated, the calcium chloride and/or magnesium chloride that abovementioned steps are obtained are (main with ammonium hydroxide
Ingredient is NH4OH) and carbon dioxide mix and carbonation reaction is carried out, the carbon dioxide recovery is converted into calcium carbonate
And/or magnesium carbonate, while generate ammonium chloride solution.Specific reaction process is shown below (to contain calcium-silicate and/or silicon containing magnesium
Exemplified by hydrochlorate is calcium silicates)：
CaCl2+2NH3+CO2+H2O→CaCO3↓+2NH4Cl
Temperature in carbonation reactor can be controlled at 20 DEG C to 95 DEG C.It, can be by step S101's in the present embodiment
The ammonia that chlorinating step generates is used to form the ammonium hydroxide in this step.
It in step S104, carries out second and separates, by the calcium carbonate and/or magnesium carbonate that are generated in step S103 point
From rear discharge.Specifically, calcium carbonate and/or magnesium carbonate are, for example, to be discharged after being settled in carbonation reactor bottom, through further
The calcium carbonate of fine particle and/or carbonic acid magnesium products can be generated after concentrate drying, become second final products, realize dioxy
Change the more stable fixation of carbon and recycling.
In step S105, carry out the recycling of ammonium chloride solution, i.e. the ammonium chloride solution that recycling step S104 is generated,
It can be directly used in after decomposition reaction generates hydrogen chloride or after concentration described in chlorination containing calcium-silicate and/or silicic acid containing magnesium
Salt, will be after the ammonium chloride solution removal partial moisture of recycling in step S101 in the present embodiment.Wherein described removal part
Moisture includes evaporating the ammonium chloride solution that the carbonation step generates, and obtains the chlorination of vapor and concentration
Ammonium salt solution, wherein the ammonium chloride solution concentrated is used for chlorination.
Further, in the present embodiment, the vapor that the evaporation step obtains also is subjected to heat by heat exchanger
Recycling.
According to the method for the recycling carbon dioxide of the present embodiment, following reaction occurs in chlorinating step：
CaSiO3+NH4Cl→CaCl2+SiO2↓+NH3↑
Following reaction occurs in carbonation step：
CaCl2+2NH3+CO2+H2O→CaCO3↓+2NH4Cl
The overall reaction of whole process is as follows：
CaSiO3+CO2→CaCO3↓+SiO2↓
By using catalyst of the ammonium chloride as entire carbon dioxide mineralising reaction, and also achieve the cycling of ammonium chloride
It uses, without lasting addition, entire technical process reduces supplies consumption compared with prior art.Catalyst in the utility model
The recycling of ammonium chloride can be realized under conditions of middle low temperature, with the prior art for example using magnesium chloride as catalyst
Technical solution compare, catalyst need not be heated to high temperature and recycled, significantly reduce the energy consumption of process.
In addition, the ammonia generated in the present embodiment in chlorinating step can be used for being formed the ammonium hydroxide in carbonation step, it is real
Existing resource maximally utilizes.The present embodiment is during the recycling of carbon dioxide is realized, reaction efficiency height, energy consumption and object
Expect at low cost, Technical Economy is more preferable.
Fig. 2 shows the flow chart of the method for the recycling carbon dioxide according to the utility model second embodiment, including
Step S201 to step S205.
In step s 201, carry out chlorination, calcium-silicate and/or chlorination containing magnesium silicate will be contained, obtain calcium chloride and/
Or magnesium chloride.In the present embodiment, chlorinating step includes will be described containing calcium-silicate and/or containing magnesium silicate and hydrogen chloride (HCl)
It reacts, in this step in addition to calcium chloride is generated, also generates silica.Specific reaction process is shown below (with calcic silicic acid
Salt and/or exemplified by being calcium silicates containing magnesium silicate)：
CaSiO3+2HCl→CaCl2+SiO2↓+H2O
Calcium silicates can be particle, hydrogen chloride can be steam or concentration for 1% to saturated concentration solution
(hydrochloric acid), reaction temperature can be at 80 DEG C to 400 DEG C.
In step S202, first time separation is carried out, is discharged after the silica generated in step S201 is separated.Specifically
Ground, what is obtained after can step S201 be reacted is passed through first with the suspension that silica dioxide granule forms by calcium chloride solution and separates
In device, silica dioxide granule is discharged after separator bottom sedimentation, and fine silica particle is generated after being further dried, into
For first final products.
In step S203, it is carbonated, the calcium chloride and/or magnesium chloride that abovementioned steps are obtained and ammonium hydroxide and two
Carbonoxide mixing and carbonation reaction, are converted into calcium carbonate and/or magnesium carbonate by the carbon dioxide recovery, while generate chlorine
Change ammonium salt solution.Specific reaction process is shown below (exemplified by containing calcium-silicate and/or be calcium silicates containing magnesium silicate)：
CaCl2+2NH3+CO2+H2O→CaCO3↓+2NH4Cl
Temperature in carbonation reactor can be controlled at 20 DEG C to 95 DEG C, obtained after reaction by ammonium chloride solution and carbon
The suspension of sour calcium solid composition.
It in step S204, carries out second and separates, by the calcium carbonate and/or magnesium carbonate that are generated in step S203 point
From rear discharge.Specifically, e.g. the above-mentioned suspension being made of ammonium chloride solution with calcium carbonate and/or magnesium carbonate solid is sent
To the second separator, the second separator separates calcium carbonate and/or magnesium carbonate solid with ammonium chloride solution, wherein calcium carbonate and/
Or magnesium carbonate can generate the calcium carbonate of fine particle and/or carbonic acid magnesium products after being further concentrated and dried, and become second
Final products realize the more stable fixation of carbon dioxide and recycling.
In step S205, carry out the recycling of ammonium chloride solution, i.e. the ammonium chloride solution that recycling step S204 is generated,
It can be directly used in after decomposition reaction generates hydrogen chloride or after concentration described in chlorination containing calcium-silicate and/or silicic acid containing magnesium
Salt, the ammonium chloride solution being isolated to the second separator in the present embodiment, after concentration, send to ammonia regenerative response
Device obtains ammonia and hydrogen chloride by decomposition reaction, wherein the hydrogen chloride decomposed is for the chlorine in step S201
Change.
Further, in the present embodiment, also by the obtained ammonia that decomposes for the institute in forming step S203
State ammonium hydroxide.
According to the method for the recycling carbon dioxide of the present embodiment, following reaction occurs in chlorinating step：
CaSiO3+2HCl→CaCl2+SiO2↓+H2O
Following reaction occurs in carbonation step：
CaCl2+2NH3+CO2+H2O→CaCO3↓+2NH4Cl
Reaction in ammonia regeneration reactor：
NH4Cl→NH3↑+HCl↑
The overall reaction of whole process is as follows：
CaSiO3+CO2→CaCO3↓+SiO2↓
By using catalyst of the ammonium chloride as entire carbon dioxide mineralising reaction, and the cycling for realizing ammonium chloride makes
With without lasting addition, entire technical process reduces supplies consumption compared with prior art.Catalyst in the utility model
The recycling of ammonium chloride can be realized under conditions of middle low temperature, it could even be possible to realizing at room temperature, with existing skill
Art compares for example with technical solution of the magnesium chloride as catalyst, need not catalyst be heated to high temperature and recycled,
Significantly reduce the energy consumption of process.
In addition, the ammonia that recycling step decomposes in the present embodiment can be used for being formed the ammonia in carbonation step
Water realizes maximally utilizing for resource.The present embodiment is during the recycling of carbon dioxide is realized, reaction efficiency is high, energy
Consumption is low with Material Cost, and Technical Economy is more preferable.
The utility model also provides a kind of system for recycling carbon dioxide, and Fig. 3 is shown according to the utility model first
The structure diagram of the system of the recycling carbon dioxide of embodiment.The system includes：Chlorination reactor 110, carbonating are anti-
Answer device 120 and retracting device 130.Chlorination reactor 110 obtains for that will contain calcium-silicate and/or chlorination containing magnesium silicate
Calcium chloride and/or magnesium chloride.Carbonation reactor 120 is connected with chlorination reactor 110, for by calcium chloride and/or magnesium chloride
With ammonium hydroxide and carbon dioxide mix and carbonation reaction, carbon dioxide fixation as calcium carbonate and/or magnesium carbonate, to be produced simultaneously
Raw ammonium chloride solution.Retracting device 130 is connected between carbonation reactor 120 and chlorination reactor 110, for recycling carbon
The ammonium chloride solution that acidification reactor 120 generates is fed directly to chlorination reaction after decomposition reaction generates hydrogen chloride or concentration
In device 110.
In the present embodiment, system further includes reducing mechanism 150, is connected with chlorination reactor 110, for by above-mentioned calcic silicon
Chlorination reactor 110 is re-fed into after hydrochlorate and/or the pulverization process of elder generation containing magnesium silicate, to improve reaction efficiency.
By there are many modes containing calcium-silicate and/or the chlorination containing magnesium silicate in chlorination reactor 110, the present embodiment
In, in chlorination reactor 110, described it will be reacted containing calcium-silicate and/or containing magnesium silicate and ammonium chloride, chlorination reactor
In 110 in addition to calcium chloride is generated, silica and ammonia are also generated.Specific reaction process is shown below (with calcic silicic acid
Salt and/or exemplified by being calcium silicates containing magnesium silicate)：
CaSiO3+NH4Cl→CaCl2+SiO2↓+NH3↑
Calcium silicates can be particle in chlorination reactor 110, and ammonium chloride can be solid powder or concentration is
1% to saturated concentration solution, 110 interior reaction temperature of chlorination reactor can be at 80 DEG C to 600 DEG C.Chlorination reactor 110 can
Think stirred tank, rotary furnace or other kinds of solid or liquid-solid reactor.By calcium chloride solution and silica dioxide granule group
Into suspension can be discharged from 110 bottom of chlorination reactor, ammonia can be from the discharge of the top of chlorination reactor 110.
The system can also include the first separator 141, be connected to chlorination reactor 110 and carbonation reactor 120
Between, the silica for chlorination reactor 110 to be generated is discharged after separating.
First separator 141 can be gas-liquid-solid three-phase separator, and temperature can be controlled at 50 DEG C to 400 DEG C.Chlorination
The suspension being made of calcium chloride solution and silica dioxide granule of 110 bottom of reactor discharge is passed through in the first separator 141,
Silica dioxide granule is discharged after being settled in 141 bottom of the first separator, and fine silica particle is generated after being further dried,
As first final products.
The particle diameter distribution of silica product can be 100nm to 1mm, and purity can be more than or equal to 80%.
In carbonation reactor 120, by calcium chloride and/or magnesium chloride and ammonium hydroxide and carbon dioxide mix and it is carbonated anti-
Should, carbon dioxide recovery is converted into calcium carbonate and/or magnesium carbonate, while generates ammonium chloride solution.Gas A can be pure two
Carbonoxide, can also any carbonated gas, enter 120 specific reaction process such as following formula of carbonation reactor from bottom
Shown (exemplified by containing calcium-silicate and/or be calcium silicates containing magnesium silicate)：
CaCl2+2NH3+CO2+H2O→CaCO3↓+2NH4Cl
Carbonation reactor 120 can be reaction and the separator of gas-liquid-solid three-phase, internal reaction temperature at 20 DEG C extremely
95 DEG C, the mineralising absorbing reaction technique in carbonation reactor 120 can operate under normal pressure, can also pressurized operation.Carbonic acid
Change the gas-liquid reactor that reactor 120 for example can be bubble tower, Airlift circulating reactor, stirred tank or other structures.The
The calcium chloride solution of one separator 141 output can be added in from the middle and upper part of carbonation reactor 120, and gas A can be pure two
Carbonoxide, can also any carbonated gas, the bottom that carbonation reactor 120 is entered from bottom is continuously added into.Through
After reaction, being purified air B can discharge from the top of carbonation reactor 120.
In the present embodiment, ammonia pipeline 170 is also set up between chlorination reactor 110 and carbonation reactor 120, by chlorine
Change the ammonia that reactor 110 generates to send into carbonation reactor 120.Ammonia pipeline 170 can be connected to carbonation reactor
120 middle part or top, ammonia meet water dissolution and obtain ammonium hydroxide.
Calcium carbonate and/or magnesium carbonate are discharged after being settled in carbonation reactor bottom, after being further concentrated and dried
The calcium carbonate of fine particle and/or carbonic acid magnesium products can be generated, become second final products, realize that carbon dioxide is relatively stablized
Fixation and recycling.
The particle diameter distribution of calcium carbonate and/or carbonic acid magnesium products can be 100nm to 1mm, and purity can be more than or equal to 80%.
Retracting device 130 is an evaporative phase-change device in the present embodiment for evaporation concentrator, evaporation concentrator temperature
It can control at 75 DEG C to 95 DEG C, pressure can be controlled in 350mbar to 850mbar, and the ammonium chloride solution of recycling is separated
For vapor and the ammonium chloride solution of concentration, wherein the ammonium chloride solution concentrated is sent to chlorination reactor 110, operated in chlorination
Middle recycling.
In the present embodiment, evaporation concentrator is also connected with heat exchanger 160, and the vapor heat that evaporation concentrator is generated returns
After receipts, the calcium chloride solution that the water that condenses out can import in the first separator 141 or directly with the outflow of the first separator mixes
After conjunction, carbonation reactor is sent into.
According to the system of the recycling carbon dioxide of the present embodiment, following reaction occurs in chlorination reactor 110：
CaSiO3+NH4Cl→CaCl2+SiO2↓+NH3↑
Following reaction occurs in 120 step of carbonation reactor：
CaCl2+2NH3+CO2+H2O→CaCO3↓+2NH4Cl
The overall reaction of whole process is as follows：
CaSiO3+CO2→CaCO3↓+SiO2↓
By using catalyst of the ammonium chloride as entire carbon dioxide mineralising reaction, and the cycling for realizing ammonium chloride makes
With without lasting addition, entire technical process reduces supplies consumption compared with prior art.Catalyst in the utility model
The recycling of ammonium chloride can be realized under conditions of middle low temperature, with the prior art for example using magnesium chloride as catalyst
Technical solution compare, catalyst need not be heated to high temperature and recycled, significantly reduce the energy consumption of process.
In addition, the ammonia generated in the present embodiment in chlorination reactor can be used for forming the ammonium hydroxide in carbonating operation,
Realize maximally utilizing for resource.The present embodiment during the recycling of carbon dioxide is realized, reaction efficiency is high, energy consumption and
Material Cost is low, and Technical Economy is more preferable.
Fig. 4 shows the structure diagram of the system of the recycling carbon dioxide according to the utility model second embodiment.
The system includes：Chlorination reactor 210, carbonation reactor 220 and retracting device 230.Chlorination reactor 210 is used to contain
Calcium-silicate and/or chlorination containing magnesium silicate obtain calcium chloride and/or magnesium chloride.Carbonation reactor 220 and chlorination reactor
210 connections, for by calcium chloride and/or magnesium chloride and ammonium hydroxide and carbon dioxide mix and carbonation reaction, by titanium dioxide
Carbon recycling is converted into calcium carbonate and/or magnesium carbonate, while generates ammonium chloride solution.Retracting device 230 is connected to carbonation reaction
Between device 220 and chlorination reactor 210, for recycling the ammonium chloride solution of the generation of carbonation reactor 220, by decomposition reaction
It is fed directly to after generation hydrogen chloride or concentration in chlorination reactor 210.
By there are many modes containing calcium-silicate and/or the chlorination containing magnesium silicate in chlorination reactor 210, the present embodiment
In, it, will be described containing calcium-silicate and/or containing magnesium silicate and hcl reaction, chlorination reactor in chlorination reactor 210
In 210 in addition to calcium chloride is generated, silica is also generated.Specific reaction process is shown below (to contain calcium-silicate and/or contain
Exemplified by magnesium silicate is calcium silicates)：
CaSiO3+2HCl→CaCl2+SiO2↓+H2O
Calcium silicates can be particle in chlorination reactor 210, hydrogen chloride can be steam or concentration for 1% to
The solution (hydrochloric acid) of saturated concentration, reaction temperature can be at 80 DEG C to 400 DEG C.Chlorination reactor 210 can be stirred tank, revolution
Stove or other kinds of solid or liquid-solid reactor.The suspension being made of calcium chloride solution and silica dioxide granule can be with
It is discharged from 210 bottom of chlorination reactor, ammonia can be from 210 top discharge of chlorination reactor.
The system can also include the first separator 241, be connected to chlorination reactor 210 and carbonation reactor 220
Between, the silica for chlorination reactor 210 to be generated is discharged after separating.First separator 241 can be gas-liquid-solid three
Phase-separating device, silica dioxide granule are discharged after being settled in 241 bottom of the first separator, and titanium dioxide is generated after being further dried
Silica fine powder particle becomes first final products.
The particle diameter distribution of silica product can be 100nm to 1mm, and purity can be more than or equal to 80%.
In carbonation reactor 220, by calcium chloride and/or magnesium chloride and ammonium hydroxide and carbon dioxide mix and it is carbonated anti-
Should, carbon dioxide recovery is converted into calcium carbonate and/or magnesium carbonate, while generates ammonium chloride solution.Specific reaction process is such as
Shown in following formula (exemplified by containing calcium-silicate and/or be calcium silicates containing magnesium silicate)：
CaCl2+2NH3+CO2+H2O→CaCO3↓+2NH4Cl
Carbonation reactor 220 can be reaction and the separator of gas-liquid-solid three-phase, internal reaction temperature at 20 DEG C extremely
95 DEG C, the mineralising absorbing reaction technique in carbonation reactor 220 can operate under normal pressure, can also pressurized operation.Carbonic acid
Change the gas-liquid reactor that reactor 220 for example can be bubble tower, Airlift circulating reactor, fluid bed or other structures.The
The calcium chloride solution of one separator 241 output can be added in from the middle and upper part of carbonation reactor 220, and gas A can be pure two
Carbonoxide, can also any carbonated gas, the bottom that carbonation reactor 220 is entered from bottom is continuously added into, ammonia
Gas or ammonium hydroxide can be added in from the middle part of carbonation reactor 220 or top.After reacted, being purified air B can be from carbon
The top discharge of acidification reactor 220.
The system can also include the first separator 242, be connected between carbonation reactor 220 and retracting device 230,
For will be discharged after calcium carbonate and/or magnesium carbonate separation.220 bottom of carbonation reactor discharge by ammonium chloride solution and carbonic acid
The suspension of calcium and/or magnesium carbonate solid composition is into the second separator 242, and the second separator 242 is by calcium carbonate and/or carbonic acid
Magnesium solid is separated with ammonium chloride solution, and wherein calcium carbonate and/or magnesium carbonate can generate fine powder after being further concentrated and dried
The calcium carbonate of grain and/or carbonic acid magnesium products become second final products, realize the more stable fixation of carbon dioxide and again profit
With.
The particle diameter distribution of calcium carbonate and/or carbonic acid magnesium products can be 100nm to 1mm, and purity can be more than or equal to 80%.
Retracting device 230 is, for example, for ammonia regeneration reactor in the present embodiment, and ammonia regeneration reactor is by recycling
Ammonium chloride solution is decomposed into ammonia and hydrogen chloride, wherein the hydrogen chloride decomposed send to chlorination reactor 210 to cycle
Carry out chlorination.Preferably, the ammonium chloride solution of recycling can carry out concentration operation before entering retracting device 230.
In the present embodiment, ammonia regeneration reactor is also connected by gas piping 280 with carbonation reactor 220, is used for
The ammonia that decomposition obtains is sent to carbonation reactor 220, ammonia meets water dissolution, becomes ammonium hydroxide.
According to the system of the recycling carbon dioxide of the present embodiment, following reaction occurs in chlorination reactor 110：
CaSiO3+2HCl→CaCl2+SiO2↓+H2O
Following reaction occurs in 120 step of carbonation reactor：
CaCl2+2NH3+CO2+H2O→CaCO3↓+2NH4Cl
Reaction in ammonia regeneration reactor：
NH4Cl→NH3↑+HCl↑
The overall reaction of whole process is as follows：
CaSiO3+CO2→CaCO3↓+SiO2↓
By using catalyst of the ammonium chloride as entire carbon dioxide mineralising reaction, and the cycling for realizing ammonium chloride makes
With without lasting addition, entire technical process reduces supplies consumption compared with prior art.Catalyst in the utility model
The recycling of ammonium chloride can be realized under conditions of middle low temperature, with the prior art for example using magnesium chloride as catalyst
Technical solution compare, catalyst need not be heated to high temperature and recycled, significantly reduce the energy consumption of process.
In addition, ammonia regeneration reactor is also connected by gas piping 280 with carbonation reactor 220 in the present embodiment,
It is sent for obtained ammonia will to be decomposed to carbonation reactor 220, for forming the ammonium hydroxide in carbonating operation, realizes resource
It maximally utilizes.The present embodiment is during the recycling of carbon dioxide is realized, reaction efficiency height, energy consumption and Material Cost
Low, Technical Economy is more preferable.
It should be noted that herein, relational terms such as first and second and the like are used merely to a reality
Body or operation are distinguished with another entity or operation, are deposited without necessarily requiring or implying between these entities or operation
In any this actual relation or order.Moreover, term " comprising ", "comprising" or its any other variant are intended to
Non-exclusive inclusion, so that process, method, article or equipment including a series of elements not only will including those
Element, but also including other elements that are not explicitly listed or further include as this process, method, article or equipment
Intrinsic element.In the absence of more restrictions, the element limited by sentence "including a ...", it is not excluded that
Also there are other identical elements in process, method, article or equipment including the element.
Embodiment according to the utility model as described above, these embodiments there is no all details of detailed descriptionthe,
Also it is only the specific embodiment not limit the utility model.Obviously, as described above, many modification and change can be made
Change.This specification is chosen and specifically describes these embodiments, and being should in order to preferably explain the principle and reality of the utility model
With so that skilled artisan can repairing using the utility model and on the basis of the utility model well
Change use.The utility model is limited only by the claims and their full scope and equivalents.
Claims (13)
1. a kind of system for recycling carbon dioxide, which is characterized in that including：
Chlorination reactor for that will contain calcium-silicate and/or chlorination containing magnesium silicate, obtains calcium chloride and/or magnesium chloride；
Carbonation reactor is connected with the chlorination reactor, for by the calcium chloride and/or magnesium chloride and ammonium hydroxide and two
Carbonoxide mixes and carries out carbonation reaction, as calcium carbonate and/or magnesium carbonate, while the carbon dioxide conversion is generated chlorine
Change ammonium salt solution；And
Retracting device is connected between the carbonation reactor and the chlorination reactor, anti-for recycling the carbonating
The ammonium chloride solution that device is answered to generate is fed directly to the chlorination reactor after decomposition reaction generates hydrogen chloride or concentration
It is interior.
2. system according to claim 1, which is characterized in that silica is also generated in the chlorination reactor, it is described
System further includes：
First separator is connected between the chlorination reactor and the carbonation reactor, for by the silica
It is discharged after separation.
3. system according to claim 1, which is characterized in that the calcium carbonate and/or magnesium carbonate pass through in the carbonic acid
Change in reactor and discharged after sedimentation separation.
4. system according to claim 1, which is characterized in that further include：
Second separator is connected between the carbonation reactor and the retracting device, for by calcium carbonate and/or carbonic acid
It is discharged after magnesium separation.
5. system according to claim 2, which is characterized in that in the chlorination reactor, described will contain calcium-silicate
And/or reacted containing magnesium silicate and ammonium chloride, also generate ammonia in the chlorination reactor.
6. system according to claim 5, which is characterized in that between the chlorination reactor and the carbonation reactor
Ammonia pipeline is also set up, the ammonia that the chlorination reactor is generated is sent into the carbonation reactor.
7. system according to claim 2, which is characterized in that the retracting device is evaporation concentrator, and the evaporation is dense
The ammonium chloride solution of recycling is separated into vapor and the ammonium chloride solution of concentration by contracting device, wherein what is concentrated is described
Ammonium chloride solution is sent to the chlorination reactor.
8. system according to claim 7, which is characterized in that the evaporation concentrator also passes through heat exchanger and described first
Separator connects.
9. system according to claim 1, which is characterized in that in the chlorination reactor, described will contain calcium-silicate
And/or it is reacted containing magnesium silicate and ammonium chloride.
10. system according to claim 1, which is characterized in that the retracting device be ammonia regeneration reactor, the ammonia
The ammonium chloride solution of recycling is decomposed into ammonia and hydrogen chloride by gas regeneration reactor, wherein the chlorination decomposed
Hydrogen is sent to the chlorination reactor.
11. system according to claim 10, which is characterized in that the ammonia regeneration reactor also by gas piping with
The carbonation reactor connection is sent for will decompose the obtained ammonia to the carbonation reactor.
12. system according to claim 1, which is characterized in that the chlorination reactor for stirred tank, rotary furnace wherein it
One.
13. system according to claim 1, which is characterized in that the carbonation reactor is bubble tower, Airlift circulating
One of reactor, fluid bed.
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