CN105258452A - Gas separation device and gas separation method for pyrolysis gas - Google Patents
Gas separation device and gas separation method for pyrolysis gas Download PDFInfo
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- CN105258452A CN105258452A CN201510724476.4A CN201510724476A CN105258452A CN 105258452 A CN105258452 A CN 105258452A CN 201510724476 A CN201510724476 A CN 201510724476A CN 105258452 A CN105258452 A CN 105258452A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 141
- 238000000926 separation method Methods 0.000 title claims abstract description 40
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 114
- 239000007789 gas Substances 0.000 claims abstract description 88
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 72
- 239000007788 liquid Substances 0.000 claims abstract description 70
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 55
- 238000005057 refrigeration Methods 0.000 claims abstract description 53
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 44
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 44
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 44
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 25
- 239000001257 hydrogen Substances 0.000 claims abstract description 24
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 24
- 239000003507 refrigerant Substances 0.000 claims abstract description 24
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000000203 mixture Substances 0.000 claims abstract description 13
- 238000000746 purification Methods 0.000 claims abstract description 11
- 239000003034 coal gas Substances 0.000 claims description 149
- 238000000034 method Methods 0.000 claims description 36
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 34
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 27
- 239000012535 impurity Substances 0.000 claims description 27
- 239000007791 liquid phase Substances 0.000 claims description 23
- 239000003245 coal Substances 0.000 claims description 21
- 230000006835 compression Effects 0.000 claims description 19
- 238000007906 compression Methods 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 18
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 18
- 229910052753 mercury Inorganic materials 0.000 claims description 18
- 229910021529 ammonia Inorganic materials 0.000 claims description 17
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 13
- 239000012071 phase Substances 0.000 claims description 13
- 229910052717 sulfur Inorganic materials 0.000 claims description 13
- 239000011593 sulfur Substances 0.000 claims description 13
- 230000015572 biosynthetic process Effects 0.000 claims description 12
- 238000005194 fractionation Methods 0.000 claims description 12
- 238000005406 washing Methods 0.000 claims description 12
- 239000002253 acid Substances 0.000 claims description 11
- 125000001741 organic sulfur group Chemical group 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 239000011280 coal tar Substances 0.000 claims description 10
- 239000007792 gaseous phase Substances 0.000 claims description 9
- 239000010687 lubricating oil Substances 0.000 claims description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 8
- 238000001035 drying Methods 0.000 claims description 8
- 238000005238 degreasing Methods 0.000 claims description 7
- 230000007062 hydrolysis Effects 0.000 claims description 7
- 238000006460 hydrolysis reaction Methods 0.000 claims description 7
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 4
- 239000000428 dust Substances 0.000 claims description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 4
- 238000011068 loading method Methods 0.000 claims description 4
- 239000011269 tar Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000000047 product Substances 0.000 description 28
- 239000003949 liquefied natural gas Substances 0.000 description 12
- 239000003463 adsorbent Substances 0.000 description 11
- 238000010521 absorption reaction Methods 0.000 description 10
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 239000000470 constituent Substances 0.000 description 5
- 229920006395 saturated elastomer Polymers 0.000 description 5
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical group CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 2
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000012190 activator Substances 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- -1 weak breath Substances 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 235000003642 hunger Nutrition 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000000192 social effect Effects 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 230000037351 starvation Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
A gas separation device for pyrolysis gas comprises a purification device and a liquefaction separation device, wherein the purification device is used for purifying the pyrolysis gas; the liquefaction separation device comprises a first heat exchanger, a first gas-liquid separator, a mixed hydrocarbon rectifying tower, a second heat exchanger, a dehydrogenation rectifying tower and a methane rectifying tower, wherein the first gas-liquid separator outputs a first mixed hydrocarbon product, the mixed hydrocarbon rectifying tower outputs a second mixed hydrocarbon product, the first heat exchanger outputs hydrogen-rich gas, and the methane rectifying tower outputs an LNG product; the liquefaction separation device also comprises a mixed refrigerant circulating refrigeration device and a nitrogen circulating refrigeration device to provide refrigeration capacity. The gas separation device for the pyrolysis gas is used for carrying out gas-liquid separation through the first gas-liquid separator, and then carrying out rectification separation for three times to obtain the hydrocarbon mixture product, the hydrogen-rich gas and the LNG product. In addition, a gas separation method of pyrolysis gas by using the device is also provided.
Description
Technical field
The present invention relates to coal chemical technology, particularly relate to a kind of gas fractionation unit and gas separating method of pyrolysis coal gas.
Background technology
The resources supplIes of " rich coal, weak breath, oil starvation ", determining energy structure in China will be long-term based on coal.Modern Coal-based Chemical is the important channel advancing Coal Clean Efficient Conversion to utilize, and the scientific and technical innovation carried out around Coal Chemical Industry and technological development, have considerable social effect and economic implications.Utilizing with the leading coal sub-prime of pulverized coal pyrolysis technology is one of important technology path of coal chemical industry.
The utilization of coal sub-prime refers to carries out pyrolysis by coal by middle low temperature distillation, takes out volatile ingredient (coal tar, coal gas) wherein, a kind of technique of residue semicoke recycling.The pyrolysis coal gas active ingredient of this process by-product is high, and wherein, methane content is more than 40%, and hydrogen rich gas content reaches 14% more than 20%, C2 ~ C5 content.
Pyrolysis coal gas is as being directly used as fuel, and its value can not make full use of, and economy is poor.Therefore, be necessary each useful constituent in pyrolysis coal gas to be separated, realize making full use of of resource, reduce the pollution to environment.
Summary of the invention
Given this, the gas fractionation unit and the gas separating method that provide a kind of pyrolysis coal gas is necessary.
A gas fractionation unit for pyrolysis coal gas, comprises purifier and liquefaction separator;
Described purifier is for purifying described pyrolysis coal gas;
Described liquefaction separator comprises First Heat Exchanger, first gas-liquid separator, mixed hydrocarbon rectifying column, second heat exchanger, dehydrogenation rectifying column and methane rectifying column, first entrance of described First Heat Exchanger is for inputting described pyrolysis coal gas, first outlet of described First Heat Exchanger is communicated with the entrance of described first gas-liquid separator, the gaseous phase outlet of described first gas-liquid separator is communicated with the entrance of described mixed hydrocarbon rectifying column, the liquid-phase outlet of described first gas-liquid separator exports the first mixed hydrocarbon product, the gaseous phase outlet of described mixed hydrocarbon rectifying column is communicated with the first entrance of described second heat exchanger, first outlet of described second heat exchanger is communicated with the entrance of described dehydrogenation rectifying column, the liquid-phase outlet of described mixed hydrocarbon rectifying column exports the second mixed hydrocarbon product, the gas vent of described dehydrogenation rectifying column is communicated with the second entrance of described second heat exchanger, second outlet of described second heat exchanger is communicated with the second entrance of described First Heat Exchanger, second outlet of described First Heat Exchanger exports hydrogen rich gas, the liquid outlet of described dehydrogenation rectifying column is communicated with the entrance of described methane rectifying column, the liquid outlet of described methane rectifying column exports LNG product, the gaseous phase outlet of described methane rectifying column is communicated with the 3rd entrance of described second heat exchanger, 3rd outlet of described second heat exchanger is communicated with the 3rd entrance of described First Heat Exchanger, 3rd outlet of described First Heat Exchanger exports tail gas,
Described liquefaction separator also comprises mixed-refrigerant cycle refrigeration plant and nitrogen circulation refrigeration plant, described mixed-refrigerant cycle refrigeration plant is used for providing cold for described pyrolyzing coal gas liquefaction, and providing cold for the overhead condenser of described mixed hydrocarbon rectifying column, described nitrogen circulation refrigeration plant is used for providing cold for the overhead condenser of described dehydrogenation rectifying column and the overhead condenser of described methane rectifying column.
Wherein in an embodiment, described purifier comprises the first compression set, degreasing unit, water washing device, pretreatment unit, the second compression set, hydrolysis device, mercury removal device, deacidifying device and the drying device that are communicated with successively;
Described first compression set is used for described pyrolyzing coal air pressure to be reduced to 0.5MPa ~ 0.8MPa;
Described degreasing unit is for removing lubricating oil in described pyrolysis coal gas and coal tar;
Described water washing device is for removing the ammonia in described pyrolysis coal gas;
Described pretreatment unit is for removing benzene in described pyrolysis coal gas and naphthalene;
Described second compression set is used for described pyrolysis coal gas to continue to be compressed to 2MPa ~ 4MPa;
It is inorganic sulfur that described hydrolysis device is used for the organic sulfur conversion in described pyrolysis coal gas;
Described mercury removal device is for removing the mercury impurities in described pyrolysis coal gas;
Described deacidifying device is for removing the acid impurities in described pyrolysis coal gas;
Described drying device is for removing the water in described pyrolysis coal gas.
Wherein in an embodiment, described mixed-refrigerant cycle refrigeration plant comprises the hybrid refrigeration compressor be communicated with successively, cooler and the second gas-liquid separator, the liquid outlet of described second gas-liquid separator is communicated with the 4th entrance of described First Heat Exchanger, 4th outlet of described First Heat Exchanger is communicated with the 5th entrance of described First Heat Exchanger, 5th outlet of described First Heat Exchanger is communicated with formation loop with described hybrid refrigeration compressor, the gas vent of described second gas-liquid separator is communicated with the 6th entrance of described First Heat Exchanger, 6th outlet of described First Heat Exchanger is communicated with the 4th entrance of described second heat exchanger, 4th outlet of described second heat exchanger is communicated with the 5th entrance of described second heat exchanger, 5th outlet of described second heat exchanger is communicated with the 5th entrance of described First Heat Exchanger, 5th outlet of described First Heat Exchanger is communicated with formation loop with described hybrid refrigeration compressor.
Wherein in an embodiment, described nitrogen circulation refrigeration plant comprises nitrogen compressor, the outlet of described nitrogen compressor is communicated with the 7th entrance of described First Heat Exchanger, 7th outlet of described First Heat Exchanger is communicated with the 6th entrance of described second heat exchanger, 6th outlet of described second heat exchanger is communicated with the entrance of current divider, first outlet of described current divider is communicated with the nitrogen inlet of the overhead condenser of described dehydrogenation rectifying column, the nitrogen outlet of the overhead condenser of described dehydrogenation rectifying column is communicated with the first entrance of the second current collector, second outlet of described current divider is communicated with the nitrogen inlet of the overhead condenser of described methane rectifying column, the nitrogen outlet of the overhead condenser of described methane rectifying column is communicated with the second entrance of described second current collector, the outlet of described second current collector is communicated with the 7th entrance of described second heat exchanger, 7th outlet of described second heat exchanger is communicated with the 8th entrance of described First Heat Exchanger, 8th outlet of described First Heat Exchanger is communicated with formation loop with the entrance of described nitrogen compressor.
A gas separating method for pyrolysis coal gas, comprises the following steps:
Purify described pyrolysis coal gas;
Pyrolysis coal gas after purification is cooled to-5 DEG C ~-25 DEG C laggard row gas-liquid separations, exports the liquid phase that gas-liquid separation obtains, obtain the first mixed hydrocarbon product;
Gas phase gas-liquid separation obtained is carried out first time rectifying and is separated, and exports first time rectifying and is separated the liquid phase obtained, and obtains the second mixed hydrocarbon product;
First time rectifying is separated the gas phase obtained and is cooled to-145 DEG C ~-165 DEG C, then, carry out second time rectifying and be separated, export after second time rectifying is separated the gas heating obtained, obtain hydrogen rich gas;
Second time rectifying is separated the liquid obtained and carries out third time rectifying separation, the liquid that output third time rectifying is separated, obtain LNG product, third time rectifying is separated the rear output of tail gas intensification obtained;
Wherein, adopt mix refrigerant to provide cold for described pyrolyzing coal gas liquefaction is separated with described first time rectifying, what adopt nitrogen to be separated with described third time rectifying for described second time rectifying separation provides cold.
Wherein in an embodiment, the operation purifying described pyrolysis coal gas comprises the following steps:
Described pyrolyzing coal air pressure is reduced to 0.5MPa ~ 0.8MPa;
Remove the lubricating oil in described pyrolysis coal gas and coal tar;
Remove the ammonia in described pyrolysis coal gas;
Remove the benzene in described pyrolysis coal gas and naphthalene;
Described pyrolysis coal gas is continued to be compressed to 2MPa ~ 4MPa;
Be inorganic sulfur by the organic sulfur conversion in described pyrolysis coal gas;
Remove the mercury impurities in described pyrolysis coal gas;
Remove the acid impurities in described pyrolysis coal gas;
Remove the water in described pyrolysis coal gas.
Wherein in an embodiment, remove in the operation of the ammonia in described pyrolysis coal gas, the method for employing washing removes the ammonia in described pyrolysis coal gas;
Remove in the operation of the mercury impurities in described pyrolysis coal gas, employing sulfur loading active carbon adsorbs the mercury impurities in described pyrolysis coal gas.
Wherein in an embodiment, mix refrigerant is adopted to provide being operating as of cold for described pyrolyzing coal gas liquefaction is separated with described first time rectifying:
After the mix refrigerant supercharging of low pressure, be cooled to 40 DEG C of laggard row gas-liquid separations, after liquid phase throttling refrigeration after gas-liquid separation, backflow as described pyrolyzing coal gas liquefaction provides rewarming after cold, after gas phase throttling refrigeration after gas-liquid separation, then backflowing provides cold for the rectifying of described first time is separated, and is mixed into described pyrolyzing coal gas liquefaction and provides rewarming after cold, backflow and form loop with the liquid phase of backflowing.
Wherein in an embodiment, adopt nitrogen to be separated with described third time rectifying for described second time rectifying is separated and being operating as of cold be provided:
Be cooled to 40 DEG C after being compressed by nitrogen, after throttling refrigeration, provide cold for described second time rectifying is separated to be separated with described third time rectifying, then backflow rewarming, formation loop.
Wherein in an embodiment, containing methane, hydrogen, C2, more than C2 component in described pyrolysis coal gas, and one or more in the component such as carbon monoxide, nitrogen, carbon dioxide, organic sulfur, sulfur dioxide, hydrogen sulfide, ammonia, tar, dust and steam, wherein, the volume content of methane is 40% ~ 45%, the volume content of hydrogen is the volume content of 20% ~ 25%, C2 ~ C5 is 10% ~ 14%.
The gas fractionation unit of above-mentioned pyrolysis coal gas and method, by purifier by after pyrolysis gas purification, gas-liquid separation is carried out again through the first gas-liquid separator, then be separated by three rectifying again and can obtain mixed hydrocarbon product, hydrogen rich gas and LNG product, appliance arrangement is uncomplicated, annexation is simple, and gas separating technology is simple, easily operates.
Accompanying drawing explanation
Fig. 1 is the structural representation of the liquefaction separator of an embodiment;
Fig. 2 is the flow chart of the gas separating method of the pyrolysis coal gas of an embodiment;
Fig. 3 is the flow chart of the purification pyrolysis coal gas of an embodiment.
Detailed description of the invention
In order to make object of the present invention, technical scheme and advantage more clear, below in conjunction with drawings and Examples, the present invention is further elaborated.Should be appreciated that specific embodiment described herein only in order to explain the present invention, be not intended to limit the present invention.
Refer to Fig. 1, the gas fractionation unit of the pyrolysis coal gas of an embodiment, comprise purifier (not shown) and liquefaction separator 100.
Purifier is for purifying pyrolysis coal gas.The volume content of active principle methane about 40% ~ 45% in pyrolysis coal gas, the volume content about 20% ~ 25% of hydrogen rich gas, the volume content about 10% ~ 14% of C2 ~ C5, also containing one or more impurity in a small amount of inert gas such as carbon monoxide, nitrogen and carbon dioxide, micro-organic sulfur, sulfur dioxide, hydrogen sulfide, ammonia, tar, dust and steam etc.
Typical pyrolysis coal gas composition is as shown in table 1, and pressure is 1 ~ 5kPa (G), and temperature is about 40 DEG C, and flow is 100000Nm
3/ h.
Table 1
| Component | Volume content (%) |
| Hydrogen | 21.34 |
| Nitrogen | 1.61 |
| Carbon monoxide | 12.77 |
| Carbon dioxide | 8.17 |
| Methane | 41.59 |
| Ethane | 5.93 |
| Ethene | 2.44 |
| Propane | 1.52 |
| Propylene | 2.03 |
| Iso-butane | 0.08 |
| Normal butane | 0.36 |
| Anti-butylene | 0.22 |
| N-butene | 0.46 |
| Isobutene | 0.3 |
| Maleic | 0.19 |
| Isopentane | 0.05 |
| Pentane | 0.14 |
| 1,3-butadiene | 0.17 |
| Ammonia | 0.07 |
| Hydrogen sulfide | 0.56 |
| Add up to | 100 |
| Tar and dust | 1.43mg/Nm 3 |
| Steam | Saturated |
Purifier comprises the first compression set, degreasing unit, water washing device, pretreatment unit, the second compression set, hydrolysis device, mercury removal device, deacidifying device and the drying device that are communicated with successively.
First compression set is used for pyrolyzing coal air pressure to be reduced to 0.5MPa ~ 0.8MPa.First compression set can be helical-lobe compressor.
Degreasing unit is for removing lubricating oil in pyrolysis coal gas and coal tar.In the present embodiment, the lubricating oil in absorption method removal pyrolysis coal gas and coal tar can be adopted.Adsorbent is the one of active carbon.This adsorbent can be with coal-based carbon raw material obtain, adsorb saturated after send coal-burning boiler to use.
Water washing device is for removing the ammonia in pyrolysis coal gas.Water washing device can be water scrubber.Adopt the ammonia in the method removing pyrolysis coal gas of washing, ammonium salt crystallization can be avoided to affect plant running.
Pretreatment unit is for removing benzene in pyrolysis coal gas and naphthalene.In the present embodiment, absorption method can be adopted to remove the heavy constituent impurity such as benzene and naphthalene in pyrolysis coal gas.Adsorbent adopts the Special adsorbent with the selective and larger adsorption capacity of good adsorption, adsorbs saturated rear high temperature regeneration, can realize recycling of adsorbent.This Special adsorbent can be the one of active carbon.
Second compression set is used for pyrolysis coal gas to continue to be compressed to 2MPa ~ 4MPa.Second compression set can be reciprocating or centrifugal compressor.
It is inorganic sulfur that hydrolysis device is used for the organic sulfur conversion in pyrolysis coal gas.In the present embodiment, medium temperature hydrolyzation technique can be adopted to be inorganic sulfur by the organic sulfur conversion in pyrolysis coal gas.
Mercury removal device is for removing the mercury impurities in pyrolysis coal gas.In the present embodiment, the Trace Mercury impurity in sulfur loading active carbon absorption pyrolysis coal gas can be adopted.
Deacidifying device is for removing the acid impurities in pyrolysis coal gas.In the present embodiment, chemical absorption method can be adopted to remove H in pyrolysis coal gas
2s, CO
2deng acid impurities.It is MDEA (N methyldiethanol amine) solution of activator that absorbent is selected with piperazine.For ensureing removal effect, the absorption and regeneration device of two cover series connection is set.After depickling, the H in pyrolysis coal gas
2s, CO
220ppm is less than Deng acid impurities content.
Drying device is for removing the water in pyrolysis coal gas.
In the present embodiment, adopt the isobaric dry absorbing process of molecular sieve, pyrolysis dew point of gas is after drying lower than-70 DEG C.
Liquefaction separator 100 comprises First Heat Exchanger 10, first gas-liquid separator 20, mixed hydrocarbon rectifying column 30, second heat exchanger 40, dehydrogenation rectifying column 50 and methane rectifying column 60.
First entrance of First Heat Exchanger 10 is for inputting pyrolysis coal gas.Arrow 1 place representative input pyrolysis coal gas in Fig. 1.First outlet of First Heat Exchanger 10 is communicated with the entrance of the first gas-liquid separator 20.First Heat Exchanger 10 can be plate-fin heat exchanger.
The gaseous phase outlet of the first gas-liquid separator 20 is communicated with the entrance of mixed hydrocarbon rectifying column 30.The liquid-phase outlet of the first gas-liquid separator 20 exports the first mixed hydrocarbon product.First mixed hydrocarbon product is C5+ component is main and containing a small amount of light component mixed hydrocarbon product.In Fig. 1, the representative of arrow 2 place exports the first mixed hydrocarbon product.
The gaseous phase outlet of mixed hydrocarbon rectifying column 30 is communicated with the first entrance of the second heat exchanger 40, and the first outlet of the second heat exchanger 40 is communicated with the entrance of dehydrogenation rectifying column 50, and the liquid-phase outlet of mixed hydrocarbon rectifying column 30 exports the second mixed hydrocarbon product.Second mixed hydrocarbon product is C3, C4 component is main and containing a small amount of C2 and C5+ mixed hydrocarbon product.In Fig. 1, the representative of arrow 3 place exports the second mixed hydrocarbon product.
The gas vent of dehydrogenation rectifying column 50 is communicated with the second entrance of the second heat exchanger 40, and the second outlet of the second heat exchanger 40 is communicated with the second entrance of First Heat Exchanger 10, and the second outlet of First Heat Exchanger 10 exports hydrogen rich gas.In Fig. 1, the representative of arrow 4 place exports hydrogen rich gas.Second heat exchanger 40 can be plate-fin heat exchanger.
The liquid outlet of dehydrogenation rectifying column 50 is communicated with the entrance of methane rectifying column 60.The liquid outlet of methane rectifying column 60 exports LNG (LiquefiedNaturalGas, liquefied natural gas) product.LNG product is sent to storage tank.In Fig. 1, the representative of arrow 5 place exports LNG product.
The gaseous phase outlet of methane rectifying column 60 is communicated with the 3rd entrance of the second heat exchanger 40, and the 3rd outlet of the second heat exchanger 40 is communicated with the 3rd entrance of First Heat Exchanger 10, and the 3rd outlet of First Heat Exchanger 10 exports tail gas.Tail gas based on carbon monoxide, and contains a small amount of hydrogen, nitrogen and trace methane.In Fig. 1, the representative of arrow 6 place exports tail gas.
Liquefaction separator 100 also comprises mixed-refrigerant cycle refrigeration plant 70 and nitrogen circulation refrigeration plant 80.Mixed-refrigerant cycle refrigeration plant 70 for providing cold for pyrolyzing coal gas liquefaction, and provides cold for the overhead condenser of mixed hydrocarbon rectifying column 30.Nitrogen circulation refrigeration plant 80 is for providing cold for the overhead condenser 52 of dehydrogenation rectifying column 50 and the overhead condenser 62 of methane rectifying column 60.
In the present embodiment, mixed-refrigerant cycle refrigeration plant 70 comprises the hybrid refrigeration compressor 72, cooler 74 and the second gas-liquid separator 76 that are communicated with successively.Cooler 74 is aftercooler.Surge tank (not shown) is also provided with before refrigeration compressor 72 entrance.
The liquid outlet of the second gas-liquid separator 76 is communicated with the 4th entrance of First Heat Exchanger 10,4th outlet of First Heat Exchanger 10 is communicated with the 5th entrance of First Heat Exchanger 10, and the 5th outlet of First Heat Exchanger 10 is communicated with formation loop with hybrid refrigeration compressor 72.Liquid phase after gas-liquid separation is lowered the temperature through First Heat Exchanger 10, again after first throttle valve 73 throttling refrigeration, then backflow as pyrolyzing coal gas liquefaction provides rewarming after cold from the 5th entrance of First Heat Exchanger 10, after flowing out from the 5th outlet of First Heat Exchanger 10, flow into surge tank, flow into hybrid refrigeration compressor 72 again, form loop.
The gas vent of the second gas-liquid separator 76 is communicated with the 6th entrance of First Heat Exchanger 10,6th outlet of First Heat Exchanger 10 is communicated with the 4th entrance of the second heat exchanger 40,4th outlet of the second heat exchanger 40 is communicated with the 5th entrance of the second heat exchanger 40,5th outlet of the second heat exchanger 40 is communicated with the 5th entrance of First Heat Exchanger 10, and the 5th outlet of First Heat Exchanger 10 is communicated with formation loop with hybrid refrigeration compressor 72.Gas phase after gas-liquid separation, successively by First Heat Exchanger 10, after second heat exchanger 40 is lowered the temperature, again through second throttle 75 throttling refrigeration, then backflow as the overhead condenser of mixed hydrocarbon rectifying column 30 provides cold from the 5th entrance of the second heat exchanger 40, after flowing out from the 5th outlet of the second heat exchanger 40, enter First Heat Exchanger 10 for pyrolyzing coal gas liquefaction from the 5th entrance of First Heat Exchanger 10 after mixing with the liquid phase of backflowing and rewarming after cold is provided, after flowing out from the 5th outlet of First Heat Exchanger 10 again, flow into surge tank, flow into hybrid refrigeration compressor 72 again, form loop.Concrete, the 5th the outlet gas phase of backflowing flowed out and the liquid phase of backflowing of the second heat exchanger 40 are at the first current collector 78 place mixing and concourse.
Nitrogen circulation refrigeration plant 80 comprises nitrogen compressor 82.Also nitrogen buffer tank is provided with before nitrogen compressor 82 entrance.The outlet of nitrogen compressor 82 is also provided with water cooler 84.The outlet of nitrogen compressor 82 is communicated with the 7th entrance of First Heat Exchanger 10.Concrete, the outlet of nitrogen compressor 82 is communicated with the 7th entrance of First Heat Exchanger 10 by water cooler 84.7th outlet of First Heat Exchanger 10 is communicated with the 6th entrance of the second heat exchanger 40.6th outlet of the second heat exchanger 40 is communicated with the entrance of current divider 90, first outlet of current divider 90 is communicated with the nitrogen inlet of the overhead condenser 52 of dehydrogenation rectifying column 50, and the nitrogen outlet of the overhead condenser 52 of dehydrogenation rectifying column 50 is communicated with the first entrance of the second current collector 95.Second outlet of current divider 90 is communicated with the nitrogen inlet of the overhead condenser 62 of methane rectifying column 60.The nitrogen outlet of the overhead condenser 62 of methane rectifying column 60 is communicated with the second entrance of the second current collector 95.The outlet of the second current collector 95 is communicated with the 7th entrance of the second heat exchanger 40, and the 7th outlet of the second heat exchanger 40 is communicated with the 8th entrance of First Heat Exchanger 10, and the 8th outlet of First Heat Exchanger 80 is communicated with formation loop with the entrance of nitrogen compressor 82.40 DEG C are cooled to after being compressed by nitrogen, lowered the temperature by First Heat Exchanger 10 and the second heat exchanger 40 successively, again by the 3rd choke valve 86 throttling refrigeration, then two strands are divided into by current divider 90, the overhead condenser 62 of the overhead condenser 52 and methane rectifying column 60 that are respectively dehydrogenation rectifying column 50 provides cold, and then return the second heat exchanger 40 and First Heat Exchanger 10 rewarming, then flow into nitrogen compressor 82 and form loop.
The gas fractionation unit of above-mentioned pyrolysis coal gas, by purifier by after pyrolysis gas purification, gas-liquid separation is carried out again through the first gas-liquid separator, then be separated by three rectifying again and can obtain mixed hydrocarbon product, hydrogen rich gas and LNG product, appliance arrangement is uncomplicated, annexation is simple, and gas separating technology is simple, easily operates.
In addition, a kind of gas separating method adopting the gas fractionation unit of above-mentioned pyrolysis coal gas to carry out pyrolysis coal gas is also provided.
Please refer to Fig. 2, in one embodiment, the gas separating method of pyrolysis coal gas, comprises the following steps:
S10, purification pyrolysis coal gas.
Please refer to Fig. 3, in the present embodiment, the operation of purification pyrolysis coal gas comprises the following steps:
S110, pyrolyzing coal air pressure is reduced to 0.5MPa ~ 0.8MPa.
In S10, adopt the first compression set that pyrolyzing coal air pressure is reduced to 0.5MPa ~ 0.8MPa.First compression set can be helical-lobe compressor.
Lubricating oil in S120, removal pyrolysis coal gas and coal tar.
The lubricating oil in degreasing unit removal pyrolysis coal gas and coal tar is adopted in S120.In the present embodiment, the lubricating oil in absorption method removing pyrolysis coal gas and coal tar is adopted.Adsorbent is active carbon, with coal-based carbon be raw material obtain, adsorb saturated after send coal-burning boiler to use.
S130, the ammonia removed in pyrolysis coal gas.
In S130, adopt the ammonia in water washing device removal pyrolysis coal gas.Adopt the ammonia in the method removing pyrolysis coal gas of washing, ammonium salt crystallization can be avoided to affect plant running.
Benzene in S140, removal pyrolysis coal gas and naphthalene.
In S140, adopt the benzene in pretreatment unit removal pyrolysis coal gas and naphthalene.In the present embodiment, absorption method can be adopted to remove the heavy constituent impurity such as benzene and naphthalene in pyrolysis coal gas.Adsorbent adopts the Special adsorbent with the selective and larger adsorption capacity of good adsorption, adsorbs saturated rear high temperature regeneration, can realize recycling of adsorbent.This Special adsorbent can be the one of active carbon.
S150, pyrolysis coal gas is continued to be compressed to 2MPa ~ 4MPa.
In S150, the second compression set is adopted to be continued to be compressed to 2MPa ~ 4MPa by pyrolysis coal gas.Second compression set can be reciprocating or centrifugal compressor.
S160, be inorganic sulfur by the organic sulfur conversion in pyrolysis coal gas.
In S160, hydrolysis device is adopted to be inorganic sulfur by the organic sulfur conversion in pyrolysis coal gas.In the present embodiment, medium temperature hydrolyzation technique can be adopted to be inorganic sulfur by the organic sulfur conversion in pyrolysis coal gas.
S170, the mercury impurities removed in pyrolysis coal gas.
In S170, adopt the mercury impurities in mercury removal device removal pyrolysis coal gas.In the present embodiment, the Trace Mercury impurity in sulfur loading active carbon absorption pyrolysis coal gas can be adopted.
S180, the acid impurities removed in pyrolysis coal gas.
In S180, adopt the acid impurities in deacidifying device removal pyrolysis coal gas.In the present embodiment, chemical absorption method can be adopted to remove H in pyrolysis coal gas
2s, CO
2deng acid impurities.It is MDEA (N methyldiethanol amine) solution of activator that absorbent is selected with piperazine.For ensureing removal effect, the absorption and regeneration device of two cover series connection is set.After depickling, the H in pyrolysis coal gas
2s, CO
220ppm is less than Deng acid impurities content.
S190, the water removed in pyrolysis coal gas.
In S190, adopt the water in drying device removal pyrolysis coal gas.
S20, the pyrolysis coal gas after purification is cooled to-5 DEG C ~-25 DEG C laggard row gas-liquid separations, exports the liquid phase that obtains of gas-liquid separation, obtain the first mixed hydrocarbon product.
In S20, First Heat Exchanger 10 is adopted to be cooled to-5 DEG C ~-25 DEG C.By mix refrigerant for pyrolyzing coal gas liquefaction provides cold.Gas-liquid separator 20 is adopted to carry out gas-liquid separation.
S30, gas phase gas-liquid separation obtained are carried out first time rectifying and are separated, and export first time rectifying and are separated the liquid phase obtained, and obtain the second mixed hydrocarbon product.
In S30, adopt mixed hydrocarbon rectifying column 30 to carry out first time rectifying and be separated.
S40, first time rectifying is separated the gas phase obtained is cooled to-145 DEG C ~-165 DEG C, then, carry out second time rectifying and be separated, export after second time rectifying is separated the gas heating obtained, obtain hydrogen rich gas.
In S40, adopt the second heat exchanger 40 that first time rectifying is separated the gas phase obtained and be cooled to-145 DEG C ~-165 DEG C.Adopt dehydrogenation rectifying column 50 to carry out second time rectifying to be separated.The hydrogen rich gas adopting the second heat exchanger 40 and First Heat Exchanger 10 second time rectifying to be separated successively to obtain heats up.Wherein, nitrogen gas refrigerant is adopted to provide cold for second time rectifying is separated.
S50, second time rectifying is separated the liquid obtained and carries out third time rectifying and be separated, export the liquid that third time rectifying is separated, obtain LNG product, third time rectifying is separated the tail gas obtained heat up after output.
In S50, adopt methane rectifying column 60 to carry out third time rectifying and be separated.The tail gas adopting the second heat exchanger 40 and First Heat Exchanger 10 third time rectifying to be separated successively to obtain heats up.Wherein, nitrogen gas refrigerant is adopted to provide cold for third time rectifying is separated.
Further, mix refrigerant is adopted to provide the operating process of cold as follows for pyrolyzing coal gas liquefaction and for the first time rectifying are separated:
After the mix refrigerant supercharging of low pressure, be cooled to 40 DEG C of laggard row gas-liquid separations, after liquid phase throttling refrigeration after gas-liquid separation, backflow as pyrolyzing coal gas liquefaction provides rewarming after cold, after gas phase throttling refrigeration after gas-liquid separation, then backflowing provides cold for first time rectifying is separated, and is mixed into pyrolyzing coal gas liquefaction and provides rewarming after cold, backflow and form loop with the liquid phase of backflowing.
Concrete, the mix refrigerant of low pressure is by hybrid refrigeration compressor 72 supercharging.40 DEG C are cooled to by cooler 74.Gas-liquid separation is carried out by the second gas-liquid separator 76.Liquid phase after gas-liquid separation, is lowered the temperature by First Heat Exchanger 10, then by first throttle valve 73 throttling, then flows back into after First Heat Exchanger 10 and pyrolysis coal gas carries out heat exchange, and rewarming flows out First Heat Exchanger 10, flows into the surge tank of hybrid refrigeration compressor 72 entrance.Gas phase after gas-liquid separation, lowered the temperature by First Heat Exchanger 10 and the second heat exchanger 40 successively, again through second throttle 75 throttling refrigeration, then flow back into the second heat exchanger 40 to be separated the hydrogen rich gas obtained to carry out heat exchange intensification with first time rectifying, flow into First Heat Exchanger 10 with after the liquid phase mixing of backflowing, flow into surge tank.
Further, nitrogen is adopted to be separated for second time rectifying and for the third time rectifying is separated and provides the operating process of cold as follows:
By nitrogen compression or be cooled to 40 DEG C, to be lowered the temperature successively, then by First Heat Exchanger 10 and the second heat exchanger 40 after the 3rd choke valve 86 throttling refrigeration, then for second time rectifying is separated and third time rectifying is separated and provides cold, then backflow rewarming, formation loop.
Nitrogen gas refrigerant, first after low-pressure nitrogen surge tank, is compressed by nitrogen compressor 82.Pressure is cooled to 40 DEG C through water cooler 84 after raising, and lowers the temperature successively through First Heat Exchanger 10 and the second heat exchanger 40, then through the 3rd choke valve 86 throttling refrigeration.Two strands are divided into by current divider 90 after throttling refrigeration, the overhead condenser 62 of the overhead condenser 52 and methane rectifying column 60 that are respectively dehydrogenation rectifying column 50 provides cold, then by the second current collector 95, return the second heat exchanger 40 and First Heat Exchanger 10 rewarming again, then flow into low-pressure nitrogen surge tank, enter nitrogen compressor 82 and form loop.
In the gas separating method of above-mentioned pyrolysis coal gas, adopt azeotrope circularly cooling and nitrogen circulation to freeze the refrigeration process combined, possess three advantages: one is that energy consumption is lower; Two is equipment mature and reliable, and manufacture craft is simple, and domestic equipment can meet the demands.For refrigeration compressor, do not have the cascade EDFA of heavy constituent cryogen be separated and complexity take out mouth, greatly reduce the manufacture requirements of compressor, be also more conducive to the stability of simplification and the dynamic equipment operation operated, thus ensure the continuous and steady operation performance of whole kind of refrigeration cycle; Three is that mix refrigerant mixes according to a certain percentage primarily of materials such as nitrogen, methane, ethene, propane, pentanes, selects more reliable.
The gas separating method of above-mentioned pyrolysis coal gas, adopt a set of optimize and combine purification, cryogenic liquefying and cryogenic rectification physical separation process program, the components such as the hydrogen in pyrolysis coal gas, methane, ethane, ethene, propane, propylene, butane, butylene, pentane are efficiently separated, produce the products such as hydrogen rich gas, LNG and mixed hydrocarbon respectively.Isolate hydrogen rich gas in pyrolysis coal gas for hydrogenation plant, LNG and mixed hydrocarbon are sold as product.By the optimum choice of process optimization and products scheme, be separated by each useful constituent in pyrolysis coal gas, the different product obtained is used respectively, has expanded the industrial chain that coal sub-prime utilizes.Compared with traditional Application way, achieve the rational and efficient use of resource, reduce the pollution to environment, create considerable economic benefit simultaneously.The gas separating method of above-mentioned pyrolysis coal gas, technological process is simple, and production cost is low, and Project Benefit is good, has the ability resisting more by force the market risk.
The above is only the preferred embodiment of the present invention; it should be pointed out that for those skilled in the art, under the premise without departing from the principles of the invention; can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (10)
1. a gas fractionation unit for pyrolysis coal gas, is characterized in that, comprises purifier and liquefaction separator;
Described purifier is for purifying described pyrolysis coal gas;
Described liquefaction separator comprises First Heat Exchanger, first gas-liquid separator, mixed hydrocarbon rectifying column, second heat exchanger, dehydrogenation rectifying column and methane rectifying column, first entrance of described First Heat Exchanger is for inputting described pyrolysis coal gas, first outlet of described First Heat Exchanger is communicated with the entrance of described first gas-liquid separator, the gaseous phase outlet of described first gas-liquid separator is communicated with the entrance of described mixed hydrocarbon rectifying column, the liquid-phase outlet of described first gas-liquid separator exports the first mixed hydrocarbon product, the gaseous phase outlet of described mixed hydrocarbon rectifying column is communicated with the first entrance of described second heat exchanger, first outlet of described second heat exchanger is communicated with the entrance of described dehydrogenation rectifying column, the liquid-phase outlet of described mixed hydrocarbon rectifying column exports the second mixed hydrocarbon product, the gas vent of described dehydrogenation rectifying column is communicated with the second entrance of described second heat exchanger, second outlet of described second heat exchanger is communicated with the second entrance of described First Heat Exchanger, second outlet of described First Heat Exchanger exports hydrogen rich gas, the liquid outlet of described dehydrogenation rectifying column is communicated with the entrance of described methane rectifying column, the liquid outlet of described methane rectifying column exports LNG product, the gaseous phase outlet of described methane rectifying column is communicated with the 3rd entrance of described second heat exchanger, 3rd outlet of described second heat exchanger is communicated with the 3rd entrance of described First Heat Exchanger, 3rd outlet of described First Heat Exchanger exports tail gas,
Described liquefaction separator also comprises mixed-refrigerant cycle refrigeration plant and nitrogen circulation refrigeration plant, described mixed-refrigerant cycle refrigeration plant is used for providing cold for described pyrolyzing coal gas liquefaction, and providing cold for the overhead condenser of described mixed hydrocarbon rectifying column, described nitrogen circulation refrigeration plant is used for providing cold for the overhead condenser of described dehydrogenation rectifying column and the overhead condenser of described methane rectifying column.
2. the gas fractionation unit of pyrolysis coal gas as claimed in claim 1, it is characterized in that, described purifier comprises the first compression set, degreasing unit, water washing device, pretreatment unit, the second compression set, hydrolysis device, mercury removal device, deacidifying device and the drying device that are communicated with successively;
Described first compression set is used for described pyrolyzing coal air pressure to be reduced to 0.5MPa ~ 0.8MPa;
Described degreasing unit is for removing lubricating oil in described pyrolysis coal gas and coal tar;
Described water washing device is for removing the ammonia in described pyrolysis coal gas;
Described pretreatment unit is for removing benzene in described pyrolysis coal gas and naphthalene;
Described second compression set is used for described pyrolysis coal gas to continue to be compressed to 2MPa ~ 4MPa;
It is inorganic sulfur that described hydrolysis device is used for the organic sulfur conversion in described pyrolysis coal gas;
Described mercury removal device is for removing the mercury impurities in described pyrolysis coal gas;
Described deacidifying device is for removing the acid impurities in described pyrolysis coal gas;
Described drying device is for removing the water in described pyrolysis coal gas.
3. the gas fractionation unit of pyrolysis coal gas as claimed in claim 1, it is characterized in that, described mixed-refrigerant cycle refrigeration plant comprises the hybrid refrigeration compressor be communicated with successively, cooler and the second gas-liquid separator, the liquid outlet of described second gas-liquid separator is communicated with the 4th entrance of described First Heat Exchanger, 4th outlet of described First Heat Exchanger is communicated with the 5th entrance of described First Heat Exchanger, 5th outlet of described First Heat Exchanger is communicated with formation loop with described hybrid refrigeration compressor, the gas vent of described second gas-liquid separator is communicated with the 6th entrance of described First Heat Exchanger, 6th outlet of described First Heat Exchanger is communicated with the 4th entrance of described second heat exchanger, 4th outlet of described second heat exchanger is communicated with the 5th entrance of described second heat exchanger, 5th outlet of described second heat exchanger is communicated with the 5th entrance of described First Heat Exchanger, 5th outlet of described First Heat Exchanger is communicated with formation loop with described hybrid refrigeration compressor.
4. the gas fractionation unit of pyrolysis coal gas as claimed in claim 1, it is characterized in that, described nitrogen circulation refrigeration plant comprises nitrogen compressor, the outlet of described nitrogen compressor is communicated with the 7th entrance of described First Heat Exchanger, 7th outlet of described First Heat Exchanger is communicated with the 6th entrance of described second heat exchanger, 6th outlet of described second heat exchanger is communicated with the entrance of current divider, first outlet of described current divider is communicated with the nitrogen inlet of the overhead condenser of described dehydrogenation rectifying column, the nitrogen outlet of the overhead condenser of described dehydrogenation rectifying column is communicated with the first entrance of the second current collector, second outlet of described current divider is communicated with the nitrogen inlet of the overhead condenser of described methane rectifying column, the nitrogen outlet of the overhead condenser of described methane rectifying column is communicated with the second entrance of described second current collector, the outlet of described second current collector is communicated with the 7th entrance of described second heat exchanger, 7th outlet of described second heat exchanger is communicated with the 8th entrance of described First Heat Exchanger, 8th outlet of described First Heat Exchanger is communicated with formation loop with the entrance of described nitrogen compressor.
5. a gas separating method for pyrolysis coal gas, is characterized in that, comprises the following steps:
Purify described pyrolysis coal gas;
Pyrolysis coal gas after purification is cooled to-5 DEG C ~-25 DEG C laggard row gas-liquid separations, exports the liquid phase that gas-liquid separation obtains, obtain the first mixed hydrocarbon product;
Gas phase gas-liquid separation obtained is carried out first time rectifying and is separated, and exports first time rectifying and is separated the liquid phase obtained, and obtains the second mixed hydrocarbon product;
First time rectifying is separated the gas phase obtained and is cooled to-145 DEG C ~-165 DEG C, then, carry out second time rectifying and be separated, export after second time rectifying is separated the gas heating obtained, obtain hydrogen rich gas;
Second time rectifying is separated the liquid obtained and carries out third time rectifying separation, the liquid that output third time rectifying is separated, obtain LNG product, third time rectifying is separated the rear output of tail gas intensification obtained;
Wherein, adopt mix refrigerant to provide cold for described pyrolyzing coal gas liquefaction is separated with described first time rectifying, what adopt nitrogen to be separated with described third time rectifying for described second time rectifying separation provides cold.
6. the gas separating method of pyrolysis coal gas as claimed in claim 5, it is characterized in that, the operation purifying described pyrolysis coal gas comprises the following steps:
Described pyrolyzing coal air pressure is reduced to 0.5MPa ~ 0.8MPa;
Remove the lubricating oil in described pyrolysis coal gas and coal tar;
Remove the ammonia in described pyrolysis coal gas;
Remove the benzene in described pyrolysis coal gas and naphthalene;
Described pyrolysis coal gas is continued to be compressed to 2MPa ~ 4MPa;
Be inorganic sulfur by the organic sulfur conversion in described pyrolysis coal gas;
Remove the mercury impurities in described pyrolysis coal gas;
Remove the acid impurities in described pyrolysis coal gas;
Remove the water in described pyrolysis coal gas.
7. the gas separating method of pyrolysis coal gas as claimed in claim 6, is characterized in that,
Remove in the operation of the ammonia in described pyrolysis coal gas, the method for employing washing removes the ammonia in described pyrolysis coal gas;
Remove in the operation of the mercury impurities in described pyrolysis coal gas, employing sulfur loading active carbon adsorbs the mercury impurities in described pyrolysis coal gas.
8. the gas separating method of pyrolysis coal gas as claimed in claim 5, is characterized in that, adopts mix refrigerant to provide being operating as of cold for described pyrolyzing coal gas liquefaction is separated with described first time rectifying:
After the mix refrigerant supercharging of low pressure, be cooled to 40 DEG C of laggard row gas-liquid separations, after liquid phase throttling refrigeration after gas-liquid separation, backflow as described pyrolyzing coal gas liquefaction provides rewarming after cold, after gas phase throttling refrigeration after gas-liquid separation, then backflowing provides cold for the rectifying of described first time is separated, and is mixed into described pyrolyzing coal gas liquefaction and provides rewarming after cold, backflow and form loop with the liquid phase of backflowing.
9. the gas separating method of pyrolysis coal gas as claimed in claim 5, is characterized in that, adopts nitrogen to be separated with described third time rectifying for described second time rectifying is separated and provides being operating as of cold:
Be cooled to 40 DEG C after being compressed by nitrogen, after throttling refrigeration, provide cold for described second time rectifying is separated to be separated with described third time rectifying, then backflow rewarming, formation loop.
10. the gas separating method of pyrolysis coal gas as claimed in claim 5, it is characterized in that, containing methane, hydrogen and C2 ~ C5 in described pyrolysis coal gas, and one or more in carbon monoxide, nitrogen, carbon dioxide, organic sulfur, sulfur dioxide, hydrogen sulfide, ammonia, tar, dust and steam, wherein, the volume content of methane is 40% ~ 45%, and the volume content of hydrogen is the volume content of 20% ~ 25%, C2 ~ C5 is 10% ~ 14%.
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| CN111320999A (en) * | 2020-03-13 | 2020-06-23 | 中国科学院过程工程研究所 | Tar component separation system and method combining fractional condensation and rectification |
| CN111320999B (en) * | 2020-03-13 | 2022-02-01 | 中国科学院过程工程研究所 | Tar component separation system and method combining fractional condensation and rectification |
| CN111517277A (en) * | 2020-05-17 | 2020-08-11 | 杨岚岚 | Water gas hydrogen production equipment for natural gas processing |
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| CN105258452B (en) | 2017-12-05 |
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