CN107118293A - A kind of method and system that polyacrylic acid is prepared with calcium carbide stove exhaust - Google Patents
A kind of method and system that polyacrylic acid is prepared with calcium carbide stove exhaust Download PDFInfo
- Publication number
- CN107118293A CN107118293A CN201710365714.6A CN201710365714A CN107118293A CN 107118293 A CN107118293 A CN 107118293A CN 201710365714 A CN201710365714 A CN 201710365714A CN 107118293 A CN107118293 A CN 107118293A
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- reactor
- tail gas
- heat
- gas
- calcium carbide
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F120/00—Homopolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride, ester, amide, imide or nitrile thereof
- C08F120/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
- C08F120/04—Acids; Metal salts or ammonium salts thereof
- C08F120/06—Acrylic acid; Methacrylic acid; Metal salts or ammonium salts thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/10—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide
- C07C51/14—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide on a carbon-to-carbon unsaturated bond in organic compounds
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
Abstract
The present invention relates to a kind of method that polyacrylic acid is prepared with calcium carbide stove exhaust, including step：High-temperature tail gas from furnace of calcium carbide is cooled down by heat exchanger, heat is delivered to carbonylation reactor and polymer reactor, for being heated to them；Dusting solid in tail gas after the cooling that exchanges heat is removed；Sulphur in tail gas after dedusting, oxygen impurities are removed；Tail gas after desulfating and deoxidation is further purified, the hydrogen and methane gas in tail gas is removed, obtains purifying CO gases；CO gases will be purified as raw material, generation acrylic acid is reacted under catalyst action with acetylene and water in carbonylation reactor；Acrylic acid is polymerized to polyacrylic acid as monomer in polymer reactor.By the above method, the present invention is utilized substantial amounts of CO gas in calcium carbide stove exhaust, obtains polyacrylic acid product.In addition, calcium carbide stove exhaust of the present invention directly exchanges heat with reactor, reactor heating is given while exhaust temperature is reduced, it is cost-effective effectively using heat.
Description
Technical field
The present invention relates to chemical field, and relate more specifically to a kind of method that polyacrylic acid is prepared with calcium carbide stove exhaust
And implement the system of this method.
Background technology
Closed type calcium carbide furnace furnace gas temperature reaches more than 1000 DEG C, and composition mainly based on CO, about accounts for 80% or so.
1 ton of calcium carbide of production will typically produce more than 400 cubic metres of furnace gas, more than 80% in so huge tail gas amount, current enterprise
Tail gas be all to be directly discharged into air.Come out of the stove due to calcium carbide production interval, light maintenance often, have a power failure, the factor such as ration the power supply, so stove
Tolerance is unstable with temperature fluctuation；Contain micro tar in furnace gas, easily make cloth bag felt jam；Dustiness is big in furnace gas, stove
Dirt has viscous, light, thin the characteristics of be difficult to flutter collection, and furnace gas has the latent heat and sensible heat of itself, is difficult to dedusting while have again
The a large amount of dust of purification.Incomplete flue gas cleaning and treatment technology are not only great waste to the energy, and environment is made
It is also sizable harm into pollution.
The content of the invention
The present invention in order to the waste gas utilization rate for solving current calcium carbide enterprise it is relatively low, pollution environment the problem of there is provided one kind at
Manage the method and system of calcium carbide stove exhaust.
There is provided a kind of method that polyacrylic acid is prepared with calcium carbide stove exhaust, including following step according to an aspect of the present invention
Suddenly：
1) tail gas exchanges heat：High-temperature tail gas from furnace of calcium carbide is subjected to cooling down by heat exchanger, heat is delivered to carbonyl
Glycosylation reaction device and polymer reactor, for carbonylation reactor and polymer reactor heating；
2) tails dedusting：By step 1) in heat exchange cooling after tail gas in dusting solid remove；
3) tail gas clean-up：By step 2) in sulphur in tail gas after dedusting, oxygen impurities removing；
4) purify：By step 3) in obtained tail gas further purify, remove the hydrogen and methane gas in tail gas, obtain
Purify CO gases；
5) it is carbonylated：Using step 4) in obtained purifying CO gases as carbonylation raw material, in carbonylation reactor with
Acetylene and water react under the catalytic action of catalyst, generate acrylic acid；
6) it polymerize：By step 5) obtained acrylic acid polymerize generation polyacrylic acid in polymer reactor.
According to one embodiment of present invention, step 2) in tails dedusting method be dry method dust and/or wet dedusting.
According to one embodiment of present invention, step 4) in remove hydrogen in tail gas and the method for methane gas be film point
From one kind in method, temp.-changing adsorption separation method, deep cooling separating method and pressure swing absorption process.
According to one embodiment of present invention, step 5) in acetylene be first dissolved in solvent and water, then with purifying CO gas
Precursor reactant.
According to one embodiment of present invention, one or more of the solvent in following：Tetrahydrofuran, 2- methyl tetrahydrochysenes
Furans, 1-METHYLPYRROLIDONE, dimethylformamide, acetone, acetylacetone,2,4-pentanedione.
According to one embodiment of present invention, step 5) in reaction temperature be 80 DEG C -120 DEG C.
According to one embodiment of present invention, step 5) in catalyst be palladium compound and organic phosphine.
According to one embodiment of present invention, step 6) in polymerisation temperature be 50 DEG C -100 DEG C.
According to another aspect of the present invention, the system that a kind of use above method prepares polyacrylic acid, the system are also provided
Including：
Heat exchanger, the gas feed of the heat exchanger is connected to calcium carbide stove exhaust pipeline；
Dust arrester, the import of the dust arrester is connected with the outlet of the heat exchanger；
Purifier, the import of the purifier is connected with the outlet of the dust arrester；
Purifying plant, the import of the purifying plant is connected with the outlet of the purifier；
Carbonylation reactor, the gas feed of the carbonylation reactor is connected with the outlet of the purifying plant, described
Carbonylation reactor also has liquid-inlet and outlet；
Polymer reactor, the import of the polymer reactor is connected with the outlet of the carbonylation reactor.
According to one embodiment of present invention, the heat transferring medium outlet connection heat exchange pipeline of heat exchanger, passes through heat exchange pipeline
Carbonylation reactor and polymer reactor are heated.
First carbonylation reactor is heated by heat exchange pipeline, then polymer reactor is heated.Heat exchange pipeline can by with
Under type is heated to reactor：Heat exchange pipeline is heated by contact and/or heat radiation to reactor；Or heat exchange pipeline and reaction
Device outer layer is connected, by the way that to reactor outer layer delivery heat transfer medium, to be heated to reactor inner chamber, the import of reactor is passed through
To reactor inner chamber.
According to one embodiment of present invention, the gas feed of carbonylation reactor is arranged on the downside of carbonylation reactor,
The liquid-inlet of carbonylation reactor is arranged on the upside of carbonylation reactor.
Using above technical scheme, the present invention has the following advantages that compared with prior art：
The present invention by the high-purity CO gases and acetylene that are obtained after calcium carbide stove exhaust purification in carbonylation reactor with
Water reaction obtains acrylic acid, and polymerization obtains polyacrylic acid.By above-mentioned processing, the present invention makes substantial amounts of carbon monoxide in tail gas
Gas is utilized；The present invention reacts acetylene dissolving in a solvent, it is to avoid the danger that acetylene explodes under high-temperature and high-pressure conditions
Danger, and ensure that bed temperature is stable, will not occur beds temperature runaway；Pass through heat exchange, the heat of the calcium carbide stove exhaust of high temperature
Measure for heating carbonylation reactor and polymer reactor, it is cost-effective effectively using heat.
Brief description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will more in the description carried out to embodiment is combined with accompanying drawing
Plus substantially and be readily appreciated that, wherein：
Fig. 1 shows the schematic flow sheet of the method that polyacrylic acid is prepared with calcium carbide stove exhaust according to the present invention；
Fig. 2 shows the schematic diagram for the system that polyacrylic acid is prepared using the method for the present invention.
Description of reference numerals
1 heat exchanger, 11 gas feeds, 12 outlets, 2 dust arresters, 21 imports, 22 outlets, 3 purifiers, 31 imports, 32
Outlet, 4 purifying plants, 41 imports, 42 outlets, 5 carbonylation reactors, 51 gas feeds, 52 liquid-inlets, 53 outlets, 6 are gathered
Close reactor, 61 imports.
Embodiment
It should be appreciated that shown embodiments of the invention are merely illustrative in the exemplary embodiment.Although in this hair
Only a small number of embodiments are described in detail in bright, but those skilled in the art are readily appreciated that and depart from the present invention in not essence
In the case of the teaching of theme, a variety of modifications are feasible.Correspondingly, all such modifications should all be included in the present invention's
In the range of.Without departing from the spirit of the invention, design, operating condition and ginseng that can be to following exemplary embodiment
Number etc. makes others and replaces, changes, changes and delete.
Solid arrow is only used for illustrating route relation in kind in Fig. 1 and Fig. 2, and dotted arrow is only used for signal heat transfer road
Line.
Reference picture 1, the present invention provides a kind of method that polyacrylic acid is prepared with calcium carbide stove exhaust, comprises the following steps：
1) tail gas exchanges heat：High-temperature tail gas from furnace of calcium carbide is subjected to cooling down by heat exchanger, heat is delivered to carbonyl
Glycosylation reaction device and polymer reactor, for carbonylation reactor and polymer reactor heating；
2) tails dedusting：By step 1) in heat exchange cooling after tail gas in dusting solid remove；
3) tail gas clean-up：By step 2) in sulphur in tail gas after dedusting, oxygen impurities removing；
4) purify：By step 3) in obtained tail gas further purify, remove the hydrogen and methane gas in tail gas, obtain
Purify CO gases；Here purifying CO gases refer to that CO gas purities reach more than 99%.
5) it is carbonylated：Using step 4) in obtained purifying CO gases as carbonylation raw material, in carbonylation reactor with
Acetylene and water react under the catalytic action of catalyst, generate acrylic acid；
6) it polymerize：By step 5) obtained acrylic acid polymerize generation polyacrylic acid in polymer reactor.
In the above-mentioned methods, step 2) in tails dedusting method be dry method dust and/or wet dedusting.
In the above-mentioned methods, step 4) in remove tail gas in hydrogen and methane gas method for membrane separating method, become
One kind in warm adsorption separating method, deep cooling separating method and pressure swing absorption process.
In the above-mentioned methods, step 5) in acetylene be first dissolved in solvent and water, then with purifying CO gas reactions.
In the above-mentioned methods, one or more of the solvent in following：Tetrahydrofuran, 2- methyltetrahydrofurans, N- first
Base pyrrolidones, dimethylformamide, acetone, acetylacetone,2,4-pentanedione.
In the above-mentioned methods, step 5) in reaction temperature be 80 DEG C -120 DEG C.
In the above-mentioned methods, step 5) in catalyst be palladium compound and organic phosphine.
In the above-mentioned methods, step 6) in polymerisation temperature be 50 DEG C -100 DEG C.
The present invention handles substantial amounts of CO gas in calcium carbide stove exhaust, tail gas using the above method and is utilized, and obtains
To polyacrylic acid product.The present invention reacts acetylene dissolving in a solvent, it is to avoid what acetylene exploded under high-temperature and high-pressure conditions
Temperature runaway phenomenon will not occur in danger, and course of reaction.In addition, high temperature calcium carbide stove exhaust of the present invention is directly changed with reactor
Heat, gives reactor heating while exhaust temperature is reduced, cost-effective effectively using heat.
In addition, reference picture 2, the present invention also provides the system that a kind of use above method prepares polyacrylic acid, the system bag
Include：
Heat exchanger 1, heat exchanger 1 has gas feed 11 and outlet 12, and gas feed 11 is connected to calcium carbide stove exhaust pipeline；
Dust arrester 2, dust arrester 2 has import 21 and outlet 22, the import 21 of dust arrester 2 and going out for heat exchanger 1
Mouth 12 is connected；
Purifier 3, purifier 3 has import 31 and outlet 32, import 31 and the dust arrester 2 of purifier 3
Outlet 22 is connected；
Purifying plant 4, purifying plant 4 has import 41 and outlet 42, import 41 and the purifier 3 of purifying plant 4
Outlet 32 is connected；
Carbonylation reactor 5, carbonylation reactor 5 has gas feed 51, liquid-inlet 52 and outlet 53, gas
Import 51 is connected with the outlet 42 of purifying plant 4, and liquid-inlet 52 is used to be passed through acetylene and water；
Polymer reactor 6, polymer reactor 6 is provided with import 61, import 61 and the phase of outlet 53 of carbonylation reactor 5
Even.
In said system, the heat transferring medium outlet connection heat exchange pipeline of heat exchanger 1 is anti-to being carbonylated by heat exchange pipeline
Device 5 and polymer reactor 6 is answered to heat successively.Certainly, heat exchange pipeline point two-way is respectively to carbonylation reactor 5 and polymer reactor
6 heating are also possible.
In said system, gas feed 51 is arranged on the downside of carbonylation reactor 5, and liquid-inlet 52 is arranged on carbonylation
The upside of reactor 5.
In embodiments of the present invention, heat exchanger 1 can be any heat exchanger used in the prior art.Such as shell and tube
Heat exchanger or coil exchanger, heat transferring medium can be water or heat-transfer oil；Dust arrester 2 is any dry method of the prior art
Or hydrofilter, purifier 3 be in the prior art be used for slough sulphur in gas, oxygen, carbon impurity any desulfurization and decarburization it is net
Change device, as long as they can realize clean-up effect simultaneously and not increase added ingredient.
In embodiments of the present invention, because exhaust temperature reaches more than 1000 DEG C, exchanged heat after the heat exchange of heat exchanger 1
The temperature of medium can reach more than 100 DEG C, and preferably 100-200 DEG C, the heat transferring medium of heat exchanger 1 with flow by controlling
The heat exchange pipeline of valve is delivered to carbonylation reactor 5 and polymer reactor 6, wherein being protected to the temperature that carbonylation reactor 5 is heated
Hold at 100 DEG C -150 DEG C, 70 DEG C -120 DEG C are maintained to the temperature that polymer reactor 6 is heated.After high-temperature tail gas is by heat exchanger 1
The heat of heat transferring medium is enough to make carbonylation reactor and polymer reactor temperature reach range of reaction temperature, without extra heat
Source, the heat of effective recycling tail gas is used for the production of acrylic acid and polyacrylic acid.
In embodiments of the present invention, the liquid-inlet 52 of carbonylation reactor 5 is in upside, and gas feed 51 is under
Side, the interior reaction temperature of carbonylation reactor 5 is controlled in the range of 80 DEG C -120 DEG C.The import 61 of polymer reactor 6 gathers in upside
The control of the interior reaction temperature of reactor 6 is closed at 50 DEG C -100 DEG C.
Here, carbonylation reactor 5 and polymer reactor 6 can be individual layer reactor of the prior art or double-deck reaction
Device, heat exchange pipeline for individual layer reactor be arranged on its periphery to heat its heat radiation or contact；For double-deck reactor,
Heat exchange pipeline is connected into outer layers delivery heat transfer medium with its outer layer to heat its internal layer by heat transferring medium, reactant is conveyed
Chemically reacted to reactor internal layer in internal layer.Hot spoke between flow or heat exchange pipeline and reactor by adjusting heat transferring medium
The heated condition to reactor can be adjusted by penetrating the size of distance, so that the temperature control of reactor is in range of reaction temperature
It is interior.It is preferred that, carbonylation reactor 5 and polymer reactor 6 are each fitted with cooling device to exceed reaction temperature in temperature of reactor
Reactor is cooled down during degree scope.It is furthermore preferred that carbonylation reactor 5 and polymer reactor 6 respectively come with agitating device,
For reaction stirred so that reaction solution is heated evenly.
Here reactor can be the paste state bed reactor for example disclosed in patent CN104826558B.
Referring to specific embodiment, the present invention will be described.
Embodiment 1
As shown in Figure 1-2, the high-temperature tail gas from furnace of calcium carbide is passed through into the cooling down of heat exchanger 1, heat passes through flow control
Valve processed is delivered to carbonylation reactor 5 and polymer reactor 6, for adding successively to carbonylation reactor 5 and polymer reactor 6
Heat, then uses pressure-variable adsorption separation side by the tail gas after the cooling that exchanges heat after dry and wet dedusting, desulfating and deoxidation purification
Method further removes the relatively low hydrogen of content and methane gas in tail gas so that tail gas is further purified, and then obtains purifying CO gas
Body.Purify CO gases to enter in carbonylation reactor 5 with dissolving acetylene in acetone and water under 90 DEG C of reaction temperatures, urging
Reaction generation acrylic acid under the catalytic action of agent palladium and triphenylphosphine.Acrylic acid is anti-at 60 DEG C in polymer reactor 6
Polymerisation generation polyacrylic acid at a temperature of answering.
Embodiment 2
As shown in Figure 1-2, the high-temperature tail gas from furnace of calcium carbide is passed through into the cooling down of heat exchanger 1, heat passes through flow control
Valve processed is delivered to carbonylation reactor 5 and polymer reactor 6, for adding successively to carbonylation reactor 5 and polymer reactor 6
Heat, then enters one after dry and wet dedusting, desulfating and deoxidation purification by the tail gas after the cooling that exchanges heat using membrane separating method
Step removes the relatively low hydrogen of content and methane gas in tail gas so that tail gas is further purified, and then obtains purifying CO gases.It is pure
Change CO gases and enter the acetylene in carbonylation reactor 5 and being dissolved in tetrahydrofuran and water under 100 DEG C of reaction temperatures, urging
Reaction generation polyacrylic acid under the catalytic action of agent palladium and 2- pyridyldiphenylphosphines.Acrylic acid is in polymer reactor 6
In under 70 DEG C of reaction temperatures polymerisation generate polyacrylic acid.
Embodiment 3
As shown in Figure 1-2, the high-temperature tail gas from furnace of calcium carbide is passed through into the cooling down of heat exchanger 1, heat passes through flow control
Valve processed is delivered to carbonylation reactor 5 and polymer reactor 6, for adding successively to carbonylation reactor 5 and polymer reactor 6
Heat, is then further removed the tail gas after the cooling that exchanges heat after dry method dust, desulfating and deoxidation purification using deep cooling separating method
The relatively low hydrogen of content and methane gas in tail gas are removed so that tail gas is further purified, and then obtains purifying CO gases.Purify CO
Gas enters the acetylene in carbonylation reactor 5 and being dissolved in 1-METHYLPYRROLIDONE and water under 110 DEG C of reaction temperatures,
Reaction generation polyacrylic acid under the catalytic action of catalyst palladium bichloride and triphenylphosphine.Acrylic acid is in polymer reactor 6 50
Polymerisation generation polyacrylic acid under DEG C reaction temperature.
Embodiment 4
As shown in Figure 1-2, the high-temperature tail gas from furnace of calcium carbide is passed through into the cooling down of heat exchanger 1, heat passes through flow control
Valve processed is delivered to carbonylation reactor 5 and polymer reactor 6, for adding successively to carbonylation reactor 5 and polymer reactor 6
Heat, is then entered the tail gas after the cooling that exchanges heat after dry and wet dedusting, desulfating and deoxidation purification using pressure swing absorption process
One step removes the relatively low hydrogen of content and methane gas in tail gas so that tail gas is further purified, and then obtains purifying CO gases.
Purifying CO gases enter the acetylene in carbonylation reactor 5 and being dissolved in acetylacetone,2,4-pentanedione and water under 80 DEG C of reaction temperatures,
Reaction generation polyacrylic acid under the catalytic action of catalyst acetic acid palladium and 2- pyridyldiphenylphosphines.Acrylic acid is in polymer reactor
Polymerisation generates polyacrylic acid under 100 DEG C of reaction temperatures in 6.
Embodiment 5
As shown in Figure 1-2, the high-temperature tail gas from furnace of calcium carbide is passed through into the cooling down of heat exchanger 1, heat passes through flow control
Valve processed is delivered to carbonylation reactor 5 and polymer reactor 6, for adding successively to carbonylation reactor 5 and polymer reactor 6
Heat, then enters one after wet dedusting, desulfating and deoxidation purification by the tail gas after the cooling that exchanges heat using variable-pressure adsorption separating method
Step removes the relatively low hydrogen of content and methane gas in tail gas so that tail gas is further purified, and then obtains purifying CO gases.It is pure
Change CO gases and enter the acetylene in carbonylation reactor 5 and being dissolved in dimethylformamide and water under 120 DEG C of reaction temperatures,
The reaction generation polyacrylic acid under the catalytic action of catalyst acetic acid palladium and diphenylphosphine.Acrylic acid in polymer reactor 6
Polymerisation generates polyacrylic acid under 90 DEG C of reaction temperatures.
As can be seen here, the present invention handles substantial amounts of CO gas in calcium carbide stove exhaust, tail gas using the above method and obtained
To utilization, polyacrylic acid product is obtained.
The foregoing is only presently preferred embodiments of the present invention, not for limit the present invention practical range；If do not taken off
From the spirit and scope of the present invention, the present invention is modified or equivalent substitution, all should covered in the claims in the present invention
Among protection domain.
Claims (10)
1. a kind of method that polyacrylic acid is prepared with calcium carbide stove exhaust, it is characterised in that comprise the following steps：
1) tail gas exchanges heat：High-temperature tail gas from furnace of calcium carbide is subjected to cooling down by heat exchanger, heat is delivered to carbonylation
Reactor and polymer reactor, for carbonylation reactor and polymer reactor heating；
2) tails dedusting：By step 1) in heat exchange cooling after tail gas in dusting solid remove；
3) tail gas clean-up：By step 2) in sulphur in tail gas after dedusting, oxygen impurities removing；
4) purify：By step 3) in obtained tail gas further purify, remove the hydrogen and methane gas in tail gas, purified
CO gases；
5) it is carbonylated：Using step 4) in obtained purifying CO gases as carbonylation raw material, with acetylene in carbonylation reactor
Reacted with water under the catalytic action of catalyst, generate acrylic acid；
6) it polymerize：By step 5) obtained acrylic acid polymerize generation polyacrylic acid in polymer reactor.
2. the method for tails dedusting is dry method dust according to the method described in claim 1, it is characterised in that the step 2)
And/or wet dedusting.
3. the hydrogen and methane gas in tail gas are removed according to the method described in claim 1, it is characterised in that the step 4)
The method of body is one kind in membrane separating method, temp.-changing adsorption separation method, deep cooling separating method and pressure swing absorption process.
4. acetylene is first dissolved in solvent and water according to the method described in claim 1, it is characterised in that the step 5),
Then with purifying CO gas reactions.
5. reaction temperature is 80 DEG C -120 DEG C according to the method described in claim 1, it is characterised in that the step 5).
6. catalyst is palladium compound and organic according to the method described in claim 1, it is characterised in that the step 5)
Phosphine.
7. the temperature of polymerisation is 50 DEG C -100 according to the method described in claim 1, it is characterised in that the step 6)
℃。
8. a kind of system that method using as any one of claim 1-7 prepares polyacrylic acid, it is characterised in that institute
The system of stating includes：
Heat exchanger, the gas feed of the heat exchanger is connected to calcium carbide stove exhaust pipeline；
Dust arrester, the import of the dust arrester is connected with the outlet of the heat exchanger；
Purifier, the import of the purifier is connected with the outlet of the dust arrester；
Purifying plant, the import of the purifying plant is connected with the outlet of the purifier；
Carbonylation reactor, the gas feed of the carbonylation reactor is connected with the outlet of the purifying plant, the carbonyl
Changing reactor also has liquid-inlet and outlet；
Polymer reactor, the import of the polymer reactor is connected with the outlet of the carbonylation reactor.
9. system according to claim 8, it is characterised in that the heat transferring medium outlet connection heat exchange pipeline of heat exchanger, leads to
The heat exchange pipeline is crossed to heat the carbonylation reactor and the polymer reactor.
10. system according to claim 8, it is characterised in that the gas feed of the carbonylation reactor is arranged on carbonyl
On the downside of glycosylation reaction device, the liquid-inlet of the carbonylation reactor is arranged on the upside of carbonylation reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710365714.6A CN107118293A (en) | 2017-05-22 | 2017-05-22 | A kind of method and system that polyacrylic acid is prepared with calcium carbide stove exhaust |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710365714.6A CN107118293A (en) | 2017-05-22 | 2017-05-22 | A kind of method and system that polyacrylic acid is prepared with calcium carbide stove exhaust |
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| Publication Number | Publication Date |
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| CN107118293A true CN107118293A (en) | 2017-09-01 |
Family
ID=59728568
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| CN201710365714.6A Pending CN107118293A (en) | 2017-05-22 | 2017-05-22 | A kind of method and system that polyacrylic acid is prepared with calcium carbide stove exhaust |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101362051A (en) * | 2008-09-27 | 2009-02-11 | 上海东化环境工程有限公司 | Acrylonitrile device tail-gas treatment technique |
| CN202700338U (en) * | 2012-08-24 | 2013-01-30 | 山西阳煤丰喜肥业(集团)有限责任公司 | Device for producing crylic acid through calcium carbide tail gas |
| CN106430202A (en) * | 2016-12-09 | 2017-02-22 | 神雾环保技术股份有限公司 | Calcium carbide production system and method |
-
2017
- 2017-05-22 CN CN201710365714.6A patent/CN107118293A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101362051A (en) * | 2008-09-27 | 2009-02-11 | 上海东化环境工程有限公司 | Acrylonitrile device tail-gas treatment technique |
| CN202700338U (en) * | 2012-08-24 | 2013-01-30 | 山西阳煤丰喜肥业(集团)有限责任公司 | Device for producing crylic acid through calcium carbide tail gas |
| CN106430202A (en) * | 2016-12-09 | 2017-02-22 | 神雾环保技术股份有限公司 | Calcium carbide production system and method |
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