CN205635417U - Clean system of natural gas system acetylene - Google Patents
Clean system of natural gas system acetylene Download PDFInfo
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- CN205635417U CN205635417U CN201620268662.1U CN201620268662U CN205635417U CN 205635417 U CN205635417 U CN 205635417U CN 201620268662 U CN201620268662 U CN 201620268662U CN 205635417 U CN205635417 U CN 205635417U
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- acetylene
- liquid
- gas
- absorption tower
- hydrogenation reactor
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- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 title claims abstract description 105
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 239000003345 natural gas Substances 0.000 title claims abstract description 23
- 239000007789 gas Substances 0.000 claims abstract description 74
- 239000007788 liquid Substances 0.000 claims abstract description 66
- 238000010521 absorption reaction Methods 0.000 claims abstract description 57
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 48
- 239000002608 ionic liquid Substances 0.000 claims description 29
- 239000003960 organic solvent Substances 0.000 claims description 12
- JKJWYKGYGWOAHT-UHFFFAOYSA-N bis(prop-2-enyl) carbonate Chemical compound C=CCOC(=O)OCC=C JKJWYKGYGWOAHT-UHFFFAOYSA-N 0.000 claims description 10
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 5
- 150000001408 amides Chemical class 0.000 claims description 4
- RAABOESOVLLHRU-UHFFFAOYSA-N diazene Chemical compound N=N RAABOESOVLLHRU-UHFFFAOYSA-N 0.000 claims description 4
- 229910000071 diazene Inorganic materials 0.000 claims description 4
- 150000002460 imidazoles Chemical class 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 3
- MKBBSFGKFMQPPC-UHFFFAOYSA-N 2-propyl-1h-imidazole Chemical compound CCCC1=NC=CN1 MKBBSFGKFMQPPC-UHFFFAOYSA-N 0.000 claims 2
- 239000002904 solvent Substances 0.000 abstract description 56
- 150000001345 alkine derivatives Chemical class 0.000 abstract description 32
- 239000012535 impurity Substances 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 abstract description 7
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 abstract description 3
- 235000012538 ammonium bicarbonate Nutrition 0.000 abstract description 3
- 239000001099 ammonium carbonate Substances 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 31
- 238000000034 method Methods 0.000 description 20
- 229910002092 carbon dioxide Inorganic materials 0.000 description 18
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 10
- 150000001335 aliphatic alkanes Chemical class 0.000 description 10
- -1 Ketohexamethylene, propylene carbonate Ester Chemical class 0.000 description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 8
- 238000000746 purification Methods 0.000 description 8
- 238000011084 recovery Methods 0.000 description 8
- LLCSWKVOHICRDD-UHFFFAOYSA-N buta-1,3-diyne Chemical group C#CC#C LLCSWKVOHICRDD-UHFFFAOYSA-N 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 230000008929 regeneration Effects 0.000 description 7
- 238000011069 regeneration method Methods 0.000 description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 238000005336 cracking Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 150000001361 allenes Chemical class 0.000 description 5
- WFYPICNXBKQZGB-UHFFFAOYSA-N butenyne Chemical group C=CC#C WFYPICNXBKQZGB-UHFFFAOYSA-N 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- MWWATHDPGQKSAR-UHFFFAOYSA-N propyne Chemical group CC#C MWWATHDPGQKSAR-UHFFFAOYSA-N 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000003556 assay Methods 0.000 description 4
- 238000010025 steaming Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- XPDWGBQVDMORPB-UHFFFAOYSA-N trifluoromethane acid Natural products FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 3
- 239000012046 mixed solvent Substances 0.000 description 3
- 230000008439 repair process Effects 0.000 description 3
- 239000001117 sulphuric acid Substances 0.000 description 3
- 235000011149 sulphuric acid Nutrition 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- LXBGSDVWAMZHDD-UHFFFAOYSA-N 2-methyl-1h-imidazole Chemical compound CC1=NC=CN1 LXBGSDVWAMZHDD-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- PAPBRGROPPJZAL-UHFFFAOYSA-N C(#N)C(CCC#N)C=1NC=CN1 Chemical compound C(#N)C(CCC#N)C=1NC=CN1 PAPBRGROPPJZAL-UHFFFAOYSA-N 0.000 description 2
- 239000005997 Calcium carbide Substances 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000008246 gaseous mixture Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000003350 kerosene Substances 0.000 description 2
- XLSZMDLNRCVEIJ-UHFFFAOYSA-N methylimidazole Natural products CC1=CNC=N1 XLSZMDLNRCVEIJ-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 description 2
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 2
- KAIPKTYOBMEXRR-UHFFFAOYSA-N 1-butyl-3-methyl-2h-imidazole Chemical class CCCCN1CN(C)C=C1 KAIPKTYOBMEXRR-UHFFFAOYSA-N 0.000 description 1
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- SJRJJKPEHAURKC-UHFFFAOYSA-N N-Methylmorpholine Chemical compound CN1CCOCC1 SJRJJKPEHAURKC-UHFFFAOYSA-N 0.000 description 1
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 1
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a clean system of natural gas system acetylene, including consecutive acetylene absorption tower, flash tank, hydrogenation ware and the carbonators that is equipped with the absorption liquid, liquid outlet on the hydrogenation ware connect in the liquid inlet on acetylene absorption tower. Clean system, the solvent can recycle, has both obtained the acetylene gas product of high -purity, can retrieve impurity changing waste into valuables again, as being used as the schizolysis raw materials behind the higher alkynes hydrogenation, CO2 and strong aqua conversion are ammonium bicarbonate.
Description
Technical field
This utility model belongs to chemical gases field of purification, particularly relates to removal and utilizes natural gas system
The system of impurity in the acetylene obtained.
Background technology
It is a series of that acetylene is widely used in synthesis acetaldehyde, acetic acid, rubber, plastics, fiber etc.
Organic products, the raw materials for production of acetylene are mainly carbide and natural gas.For a long time, domestic base
It is all to use calcium carbide method acetylene production in basis.But along with aggravation and the cleaning of Global Greenhouse Effect are raw
Going deep into of product theory, calcium carbide method acetylene production is by more and more difficult.Abroad make raw material with natural gas
Produce acetylene accounts for 1/4, to account for 3/4 in the U.S., and China is then less than 5%.Along with people's environment
Constantly strengthening of consciousness and becoming increasingly abundant, with natural gas for raw material production acetylene of natural gas resource
Acetylene industrial expansion trend will be become, there is the bright outlook.
Natural gas produces acetylene volume fraction only 8%～15% in the gas of acetylene, and remaining is
Impurity.Impurity in acetylene unstripped gas is mainly by H, CH, CO, CO2Etc. light component (generally
Be referred to as fixed gas) and diacetylene, butadiene, vinylacetylene, allene, allylene,
The heavy constituents such as C6+ (commonly referred to higher alkyne) form.These impurity Downstream processing to acetylene
Utilizing impact very big, light component can reduce conversion of alkyne, and heavy constituent not only makes catalyst poisoning,
And it is (especially diacetylene) poor stability, easily polymerization blocking pipeline and equipment, inflammable and explosive.
In order to improve the purity of acetylene, make acetylene can be suitably used for ethylene processed, acrylic acid, vinyl acetate and
The chemical products such as BDO require higher chemical process to purity acetylene, it is necessary to right
The acetylene that gas by partial oxidation of natural prepares purifies, and removes higher alkyne, clean to reach acetylene
Change and require >=99.5%.
The main method removing senior unsaturated hydrocarbons at present from acetylene unstripped gas is that concentrated sulphuric acid is washed
Washing method, wherein higher alkyne is oxidized to water and CO by the concentrated sulphuric acid of 98%2, finally with acid sludge
Form is discharged, CO2By alkali liquor (NaOH or Na2CO3) neutralize removing, purity can be obtained and be more than
The acetylene product of 99.5%.Although sulfuric acid scrubbing method can obtain acetylene product up to standard, but exists
The problems such as acid and alkali consumption amount is big, spent acid is difficult.Acetylene purification method is except concentrated sulphuric acid washing method
Also having absorption method and solvent method, absorption method is to utilize adsorbent to the absorbability of different component not
With, convert pressure or temperature to realize the adsorbent absorption to target affinity molecule by suitable
And desorption manipulation, use the higher hydrocarbons in alternating temperature pressure swing adsorption technique removing acetylene unstripped gas,
The product acetylene of purity ＞ 99.4% can be obtained.But such method exist adsorbent be difficult to regeneration,
CO in corrosion-resistant requirement acetylene high, dense2Alkynes during, high temperature regeneration the highest with ethylene contents
The problems such as easy polymerization, the most industrial large-scale plant not having adsorption method for purifying acetylene.Solvent method
It is to utilize solvent different, (such as temperature under different operating conditions to the selectivity of higher alkyne
Degree, pressure) carry out absorbing or desorbing, thus imurity-removal.The solvent of commercial Application have NMP,
DMF, methanol, liquefied ammonia, kerosene, diesel oil etc., higher alkyne is all had higher dissolubility and
Selectivity.Wherein the alkalescence solvent such as NMP, DMF, methanol big to higher alkyne dissolubility,
Solvent load is little, but easily causes acetylene loss, and NMP and DMF desorption condition is harsh, needs
High temperature and vacuum；The selectivity of higher alkyne is lost by kerosene and diesel oil much larger than acetylene, acetylene
Little, but solvent circulating load is big, and diesel oil also needs to absorb at a lower temperature.There is patent report
The solvent of other selectively removing higher alkynes, such as methyl morpholine, Ketohexamethylene, propylene carbonate
Ester etc., but have no its relevant pilot scale or commercial Application report.It addition, higher alkyne character pole
Unstable, it is easy to decompose (decomposition pressure such as diacetylene is only 0.02MPa), and nothing
The combustion explosion upper limit, produces to enterprise and brings the biggest potential safety hazard.These by-product higher alkynes are big
Part is all material gas, and content is huge, if directly sending boiler or torch burning, is
Serious waste to resource.
This utility model provides the purification technique of a kind of natural gas acetylene, selects a kind of novel
Mixed solvent removes higher alkyne and CO2, same ensureing that purification acetylene product quality requires
Time, the Waste Sulfuric Acid pollution to environment and the loss of higher alkyne can be avoided, simultaneously by the height of abjection
Level alkynes obtains normal butane and propane by hydrogenation, is used for doing cracking stock, improves higher alkyne
Added value rather than directly burn as fuel；CO2React with strong aqua ammonia and obtain bicarbonate
Ammonium is used for making chemical fertilizer rather than being directly discharged in air.
Utility model content
(1) to solve the technical problem that
For prior art uses the senior unsaturated hydrocarbons in dense sulfuric acid treatment acetylene unstripped gas
The problems such as the acid and alkali consumption amount existed is big, spent acid is difficult, this utility model provides one to process
The system of the hydrocarbon impurities in acetylene production.
(2) technical scheme
Cleaning system described in the utility model, including the acetylene equipped with absorbing liquid being sequentially connected
Absorption tower, flash tank, hydrogenation reactor and carbonators；Liquid discharge on described hydrogenation reactor
Mouth is connected to the liquid inlet of described acetylene absorption tower.
System described in the utility model, also includes being connected to described flash tank and described hydrogenation is anti-
The regenerator between device, the gas outlet on described regenerator is answered to be connected to described acetylene absorption tower
Gas access.
System described in the utility model, the liquid outlet on described hydrogenation reactor and described second
It is provided with Control device of liquid cooling between the liquid inlet on alkynes absorption tower.
System described in the utility model, also sets between described hydrogenation reactor and described carbonators
There is the cooler and gas-liquid separator being sequentially connected.
System described in the utility model, its structure is preferably:
Including the acetylene absorption tower equipped with absorbing liquid being sequentially connected, flash tank, hydrogenation reactor
And carbonators；
Also include the regenerator being connected between described flash tank and described hydrogenation reactor, described
Gas outlet on regenerator is connected to the gas access of described acetylene absorption tower；
Liquid outlet on described hydrogenation reactor is connected to the liquid of described acetylene absorption tower and enters
Mouthful；The cooler being sequentially connected it is additionally provided with gentle between described hydrogenation reactor and described carbonators
Liquid/gas separator；Liquid outlet on described hydrogenation reactor enters with the liquid of described acetylene absorption tower
Control device of liquid cooling it is provided with between Kou；
Described absorbing liquid is 1,3-diacetayl amide imidazoles diimine ionic liquid, 1-acetamide-3
One or both in Methylimidazole. ionic liquid and 1,3-dicyan propyl imidazole ionic liquid；Institute
Stating organic solvent is N methyldiethanol amine (MDEA), 1,8-diazabicyclo [5,4,0] ten
One or both in one carbon-7-alkene (DBU), Allyl carbonate；Wherein, described organic
The percent by volume of solvent is 5～50%.
The using method of system described in the utility model, comprises the steps:
1) product that natural gas oxicracking obtains is passed through acetylene absorption tower, acetylene therein,
Carbon dioxide and other alkynes are absorbed by liquid absorption, and can not discharge acetylene absorption by absorbed gas
Tower；
2) described absorbing liquid is passed through flash tank, goes out acetylene by flash separation, obtain acetylene
Finished product and the absorbing liquid of removal acetylene；
3) absorbing liquid of described removal acetylene is passed through hydrogenation reactor, carries out hydrogenation reaction,
Obtain alkanes gas and CO2Gaseous mixture；
4) described gaseous mixture is passed through described carbonators, CO2Reaction generates ammonium hydrogen carbonate, real
Existing alkanes gas and CO2Separation.
Preferably, carrying out step 3) described in hydrogenation reaction before, by described step 2) in
Acetylene absorption liquid is first passed through regenerator, parses the acetylene of residual；Control the behaviour of described regenerator
Being 100～120 DEG C as temperature, operation pressure is 0.1～0.6MPa, obtains admixture of gas and connects
Gas access to absorption tower.
In this utility model, described absorbing liquid is the mixed solution of ionic liquid and organic solvent,
Described ionic liquid is 1,3-diacetayl amide imidazoles diimine ionic liquid, 1-acetamide-3
One or both in Methylimidazole. ionic liquid and 1,3-dicyan propyl imidazole ionic liquid；Institute
Stating organic solvent is N methyldiethanol amine (MDEA), 1,8-diazabicyclo [5,4,0] ten
One or both in one carbon-7-alkene (DBU), Allyl carbonate；Wherein, described organic
The percent by volume of solvent is 5～50%.
In this utility model, in acetylene absorption tower, controlling gas space velocity is 500～750Nm3/ h,
Liquid air speed is 5～7.5m3/ h, operation temperature is 15～35 DEG C, and pressure is 0～0.500MPa
In this utility model, during carrying out flash distillation, controlling temperature is 20～40 DEG C, pressure
Power is 0.08～0.11MPa.
In this utility model, higher alkyne and hydrogen are 50～130 DEG C in operation temperature, operation
Pressure is to carry out hydrogenation reaction under conditions of 0～0.5Mpa.
In this utility model, the operation temperature of carbonators is 50～80 DEG C, and operation pressure is
0～0.4Mpa.
(3) beneficial effect
Method described in the utility model has the advantages that
(1) system of natural gas acetylene of the present utility model need not by arrange washing,
The steps such as rectification realize recycling of solvent, and solvent cycle cost is low, can reduce solvent simultaneously
Loss；
(2) solvent uses ionic liquid and the mixture of organic solvent, has both avoided ionic liquid
The high viscosity of body, poor fluidity and the volatilization of organic solvent height, high consumption, the difficult deficiency reclaimed,
The regeneration that can realize again solvent by the way of heating under reduced pressure recycles, and is regenerating
Product will not be polluted by journey；
(3) mixture of ionic liquid and organic solvent is nontoxic, non-corrosiveness, to equipment material
Matter is less demanding, absorbs the gentleest with regeneration condition, acetylene loss low (less than 0.5%, volume
Mark)；
(4) hydrogenation reaction of higher alkyne and a small amount of acetylene and the regeneration of solvent are integrated in one
Carrying out in individual reactor, the higher alkyne being not only dissolved in solvent carries out catalytic hydrogenation and turns
Change, again solvent is regenerated, it is achieved that catalytic reaction and regenerative process the most integrated；
(5) solvent can recycle, and has both obtained highly purified acetylene gas product, can make again
The impurity reclaimed is turned waste into wealth, and is used as cracking stock, CO after being hydrogenated with such as higher alkyne2With dense ammonia
Water reaction is converted into ammonium hydrogen carbonate, is used as chemical fertilizer；
Accompanying drawing explanation
Fig. 1: for the cleaning system schematic diagram of a kind of natural gas acetylene；
In figure: 1, acetylene absorption tower；2, rich solvent pump；3, flash tank；4, regenerator；
5, hydrogenation reactor；6, condenser；7, gas-liquid separator；8, carbonators；9, regeneration
Gas outlet on tower；10, the gas access of acetylene absorption tower；11, the liquid of hydrogenation reactor
Body exports；12, the liquid inlet of acetylene absorption tower；13, Control device of liquid cooling.
Detailed description of the invention
Following example are used for illustrating this utility model, but are not limited to model of the present utility model
Enclose.
Embodiment 1
The present embodiment relates to a kind of system utilizing natural gas incomplete oxidation acetylene, its structure
Schematic diagram is as shown in Figure 1:
Including the acetylene absorption tower 1 equipped with absorbing liquid being sequentially connected, flash tank 3, hydrogenation reaction
Device 5 and carbonators 8；Liquid outlet 11 on described hydrogenation reactor is connected to described acetylene absorption
The liquid inlet 12 of tower.
Regenerator 4, described regenerator 4 it is provided with between described flash tank 3 and described hydrogenation reactor 5
On gas outlet 9 be connected to the gas access 10 of described acetylene absorption tower.
Embodiment 2
Compared with Example 1, its difference is, the liquid outlet 11 on described hydrogenation reactor 5
And it is provided with Control device of liquid cooling 13 between the liquid inlet 12 of described acetylene absorption tower.
Be additionally provided with between described hydrogenation reactor and described carbonators the cooler 6 being sequentially connected and
Gas-liquid separator 7.
Embodiment 3
The present embodiment relates to the use of what system purification natural-gas described in the utility model prepared
In acetylene, the method for impurity, comprises the steps:
1) product that natural gas oxicracking obtains is passed through acetylene absorption tower, absorbed liquid portion
Divide and absorb, acetylene absorption tower can not be discharged by absorbed gas；The air speed of described unstripped gas is
600Nm3/ h, the pressure in absorption tower is 0.45MPa, gas consist of containing 7.8% (mole
Concentration, lower same) C2H2, 4.9%CH4, 0.2%C2H4, 25.7%CO, 0.9%N2, 55.9%H2、
3.3%CO2, 1.2% higher alkyne and other a small amount of C6 +Above component.Absorbing liquid is 1,3-
Double (fluoroform sulphonyl) the inferior amine salt ionic liquid of diacetayl amide imidazoles and the mixing of Allyl carbonate
Solvent, its flow velocity is 5m3/ h, wherein the mass content of Allyl carbonate is 50%, and remaining is
Double (fluoroform sulphonyl) the inferior amine salt ionic liquid of 1,3-diacetayl amide imidazoles, gas is at 25 DEG C
Contact absorption with cracking gas back flow of gas, acetylene absorption tower (2) tower top obtains the lowest
The H of dissolubility2、CO、N2Residual exhaust Deng gas；
2) C is absorbed2H2、CH4, higher alkyne, CO2And C2H4Absorbing liquid Deng material
Send into flash tank by rich solvent pump 2, flash off the acetylene in solvent, deliver to product gas；Dodge
The operation temperature of steaming pot is 30 DEG C, and operation pressure is 0.1MPa；
3) solvent bottom flash tank is passed through regenerator, parses the acetylene etc. of residual in solvent
Gas, passes to the gas access on absorption tower again, and regenerator operation temperature is 110 DEG C, operation
Pressure is 0.5MPa；
4) the solvent entrance hydrogenation reactor at the bottom of regenerator tower carries out catalytic hydrogenation reaction, alkynes
Class material is changed to positive butane and propane after crossing catalytic hydrogenation, a small amount of acetylene catalytic hydrogenation is raw
Become ethylene；Hydrogenation reactor is by the catalytic hydrogenation reaction of higher alkyne and a small amount of acetylene and solvent
Regeneration is integrated in a reactor and carries out, and the higher alkyne being not only dissolved in solvent is carried out
Catalytic hydroconversion, is regenerated solvent again, it is achieved that catalytic reaction and regenerative process
The most integrated, the temperature of hydrogenation reaction is 120 DEG C, and operation pressure is 0.4MPa, after hydrogenation
Gaseous product is condensed, after separation and recovery solvent, obtain alkanes gaseous product；
5) described alkanes gaseous product enters carbonators, and the operation temperature of carbonators is 60 DEG C,
Operation pressure is 0.3MPa.
After assay device is stable, the content obtaining gas acetylene is 99.8% (volume basis
Than), the yield of acetylene is 97.1%, diacetylene, butadiene, vinylacetylene, allene,
Allylene and CO2Content for reducing to 0, and achieve the recovery of solvent.
Embodiment 4
The present embodiment relates to the use of what system purification natural-gas described in the utility model prepared
In acetylene, the method for impurity, comprises the steps:
1) product that natural gas oxicracking obtains is passed through acetylene absorption tower, absorbed liquid portion
Divide and absorb, acetylene absorption tower can not be discharged by absorbed gas；The air speed of described unstripped gas is
600Nm3/ h, the pressure in absorption tower is 0.45MPa, gas consist of containing 7.8% (mole
Concentration, lower same) C2H2, 4.9%CH4, 0.2%C2H4, 25.7%CO, 0.9%N2, 55.9%H2、
3.3%CO2, 1.2% higher alkyne and other a small amount of C6 +Above component.Absorbing liquid is 1,3-
Double (fluoroform sulphonyl) the inferior amine salt ionic liquid of diacetayl amide imidazoles and the mixing of Allyl carbonate
Solvent, wherein the mass content of Allyl carbonate is 5%, and remaining is 1, and 3-diacetayl amide imidazoles is double
(fluoroform sulphonyl) inferior amine salt ionic liquid, liquid air speed is 5m3/ h, gas at 25 DEG C with
The contact of cracking gas back flow of gas absorbs, and acetylene absorption tower (2) tower top obtains the lowest molten
The H of Xie Du2、CO、N2Residual exhaust Deng gas；
2) C is absorbed2H2、CH4, higher alkyne, CO2And C2H4Absorbing liquid Deng material
Send into flash tank by rich solvent pump 2, flash off the acetylene in solvent, deliver to product gas；Dodge
The operation temperature of steaming pot is 30 DEG C, and operation pressure is 0.1MPa；
3) solvent bottom flash tank is passed through regenerator, parses the acetylene etc. of residual in solvent
Gas, passes to the gas access on absorption tower again, and regenerator operation temperature is 110 DEG C, operation
Pressure is 0.5MPa；
4) the solvent entrance hydrogenation reactor at the bottom of regenerator tower carries out catalytic hydrogenation reaction, hydrogenation
The temperature of reaction is 120 DEG C, and operation pressure is 0.4MPa, the gaseous product after hydrogenation is condensed,
After separation and recovery solvent, obtain alkanes gaseous product；
5) described alkanes gaseous product enters carbonators, and the operation temperature of carbonators is 60 DEG C,
Operation pressure is 0.3MPa.
After assay device is stable, the content obtaining gas acetylene is 97.6% (volume basis
Than), the yield of acetylene is 93.1%, diacetylene, butadiene, vinylacetylene, allene and
Allylene removal efficiency is respectively 97.1%, 98.3%, 97.4%, 98.7% and 99.2%, CO2
Content for reducing to 0, and achieve the recovery of solvent.
Embodiment 5
The present embodiment relates to the use of what system purification natural-gas described in the utility model prepared
In acetylene, the method for impurity, comprises the steps:
1) product that natural gas oxicracking obtains is passed through acetylene absorption tower, absorbed liquid portion
Divide and absorb, acetylene absorption tower can not be discharged by absorbed gas；The air speed of described unstripped gas is
600Nm3/ h, the pressure in absorption tower is 0.45MPa, gas consist of containing 7.8% (mole
Concentration, lower same) C2H2, 4.9%CH4, 0.2%C2H4, 25.7%CO, 0.9%N2, 55.9%H2、
3.3%CO2,1.2% higher alkyne and other a small amount of more than C6+ components.Absorbing liquid is 1-second
Amide-3 Methylimidazole. ionic liquid and the mixed solvent of N methyldiethanol amine (MDEA),
Wherein the mass content of MDEA is 10%, and remaining is 1-butyl-3-methylimidazole salt ionic liquid
Body, liquid air speed is 5m3/ h, gas contacts absorption with cracking gas back flow of gas at 25 DEG C,
Acetylene absorption tower (2) tower top obtains the H of low solubility in a solvent2、CO、N2Deng gas
Residual exhaust；
2) C is absorbed2H2、CH4, higher alkyne, CO2And C2H4Absorbing liquid Deng material
Send into flash tank by rich solvent pump 2, flash off the acetylene in solvent, deliver to product gas；Dodge
The operation temperature of steaming pot is 30 DEG C, and operation pressure is 0.1MPa；
3) solvent bottom flash tank is passed through regenerator, parses the acetylene etc. of residual in solvent
Gas, passes to the gas access on absorption tower again, and regenerator operation temperature is 110 DEG C, operation
Pressure is 0.5MPa；
4) the solvent entrance hydrogenation reactor at the bottom of regenerator tower carries out catalytic hydrogenation reaction, hydrogenation
The temperature of reaction is 120 DEG C, and operation pressure is 0.4MPa, the gaseous product after hydrogenation is condensed,
After separation and recovery solvent, obtain alkanes gaseous product；
5) described alkanes gaseous product enters carbonators, and the operation temperature of carbonators is 60 DEG C,
Operation pressure is 0.3MPa.
After assay device is stable, the content obtaining gas acetylene is 99.3% (volume basis
Than), the yield of acetylene is 96.2%, diacetylene, butadiene, vinylacetylene, allene and
Allylene removal efficiency is respectively 99.1%, 99.3%, 99.4%, 99.7% and 99.2%, CO2
Content for reducing to 0.1%, and achieve the recovery of solvent.
Embodiment 6
The present embodiment relates to the use of what system purification natural-gas described in the utility model prepared
In acetylene, the method for impurity, comprises the steps:
1) product that natural gas oxicracking obtains is passed through acetylene absorption tower, absorbed liquid portion
Divide and absorb, acetylene absorption tower can not be discharged by absorbed gas；The air speed of described unstripped gas is
600Nm3/ h, the pressure in absorption tower is 0.45MPa, gas consist of containing 7.8% (mole
Concentration, lower same) C2H2, 4.9%CH4, 0.2%C2H4, 25.7%CO, 0.9%N2, 55.9%H2、
3.3%CO2,1.2% higher alkyne and other a small amount of C6 +Above component.Absorbing liquid is 1-second
Amide-3 Methylimidazole. ionic liquid and the mixed solvent of Allyl carbonate, wherein Allyl carbonate
Mass content be 5%, remaining is 1-acetamide-3 Methylimidazole. ionic liquid, and liquid air speed is
5m3/ h, gas contacts absorption, acetylene absorption tower (2) at 25 DEG C with cracking gas back flow of gas
Tower top obtains the H of low solubility in a solvent2、CO、N2Residual exhaust Deng gas；
2) C is absorbed2H2、CH4, higher alkyne, CO2And C2H4Absorbing liquid Deng material
Send into flash tank by rich solvent pump 2, flash off the acetylene in solvent, deliver to product gas；Dodge
The operation temperature of steaming pot is 30 DEG C, and operation pressure is 0.1MPa；
3) solvent bottom flash tank is passed through regenerator, parses the acetylene etc. of residual in solvent
Gas, passes to the gas access on absorption tower again, and regenerator operation temperature is 110 DEG C, operation
Pressure is 0.5MPa；
4) the solvent entrance hydrogenation reactor at the bottom of regenerator tower carries out catalytic hydrogenation reaction, hydrogenation
The temperature of reaction is 120 DEG C, and operation pressure is 0.4MPa, the gaseous product after hydrogenation is condensed,
After separation and recovery solvent, obtain alkanes gaseous product；
5) described alkanes gaseous product enters carbonators, and the operation temperature of carbonators is 60 DEG C,
Operation pressure is 0.3MPa.
After assay device is stable, the content obtaining gas acetylene is 99.5% (volume basis
Than), the yield of acetylene is 96.4%, diacetylene, butadiene, vinylacetylene, allene and
Allylene removal efficiency is respectively 99.5%, 99.8%, 99.7%, 99.9% and 99.6%, CO2
Content for reducing to 0, and achieve the recovery of solvent.
Although, used general explanation, detailed description of the invention and test, to this reality
Made detailed description with novel, but on the basis of this utility model, can to work some repair
Changing or improve, this will be apparent to those skilled in the art.Therefore, without departing from
These modifications or improvements on the basis of this utility model spirit, belong to this utility model
Claimed scope.
Claims (6)
1. the cleaning system of a natural gas acetylene, it is characterised in that include acetylene absorption tower, flash tank, hydrogenation reactor and the carbonators equipped with absorbing liquid being sequentially connected；Liquid outlet on described hydrogenation reactor is connected to the liquid inlet of described acetylene absorption tower.
System the most according to claim 1, it is characterised in that also include the regenerator being connected between described flash tank and described hydrogenation reactor, the gas outlet on described regenerator is connected to the gas access of described acetylene absorption tower.
System the most according to claim 1 and 2, it is characterised in that be provided with Control device of liquid cooling between liquid outlet and the liquid inlet of described acetylene absorption tower on described hydrogenation reactor.
System the most according to claim 3, it is characterised in that be additionally provided with the cooler being sequentially connected and gas-liquid separator between described hydrogenation reactor and described carbonators.
System the most according to claim 1 and 2, it is characterized in that, described absorbing liquid is the mixed solution of ionic liquid and organic solvent, described ionic liquid is 1,3-diacetayl amide imidazoles diimine ionic liquid, 1-acetamide-3 Methylimidazole. ionic liquid and 1, one or both in 3-dicyan propyl imidazole ionic liquid；Described organic solvent is one or both in N methyldiethanol amine, 1,8-diazabicyclo [5,4,0] 11 carbon-7-alkene, Allyl carbonate；Wherein, the percent by volume of described organic solvent is 5～50%.
System the most according to claim 1, it is characterised in that
Also including the regenerator being connected between described flash tank and described hydrogenation reactor, the gas outlet on described regenerator is connected to the gas access of described acetylene absorption tower；
Liquid outlet on described hydrogenation reactor is connected to the liquid inlet of described acetylene absorption tower；The cooler being sequentially connected and gas-liquid separator it is additionally provided with between described hydrogenation reactor and described carbonators；It is provided with Control device of liquid cooling between liquid outlet and the liquid inlet of described acetylene absorption tower on described hydrogenation reactor；
Described absorbing liquid is the mixed solution of ionic liquid and organic solvent, and described ionic liquid is 1,3-diacetayl amide imidazoles diimine ionic liquid, 1-acetamide-3 Methylimidazole. ionic liquid and 1, one or both in 3-dicyan propyl imidazole ionic liquid；Described organic solvent is one or both in N methyldiethanol amine, 1,8-diazabicyclo [5,4,0] 11 carbon-7-alkene, Allyl carbonate；Wherein, the percent by volume of described organic solvent is 5～50%.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107954820A (en) * | 2016-10-17 | 2018-04-24 | 中国石油化工股份有限公司 | A kind of method for removing the thick middle-and-high-ranking alkynes of acetylene gas |
| CN114887344A (en) * | 2022-05-10 | 2022-08-12 | 福建福豆新材料有限公司 | Industrial acetylene purification device and method for purifying industrial acetylene by using same |
-
2016
- 2016-03-31 CN CN201620268662.1U patent/CN205635417U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107954820A (en) * | 2016-10-17 | 2018-04-24 | 中国石油化工股份有限公司 | A kind of method for removing the thick middle-and-high-ranking alkynes of acetylene gas |
| CN114887344A (en) * | 2022-05-10 | 2022-08-12 | 福建福豆新材料有限公司 | Industrial acetylene purification device and method for purifying industrial acetylene by using same |
| CN114887344B (en) * | 2022-05-10 | 2023-11-03 | 福建福豆新材料有限公司 | Method for purifying industrial acetylene by using industrial acetylene purifying device |
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