CN105258452B - 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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- CN105258452B CN105258452B CN201510724476.4A CN201510724476A CN105258452B CN 105258452 B CN105258452 B CN 105258452B CN 201510724476 A CN201510724476 A CN 201510724476A CN 105258452 B CN105258452 B CN 105258452B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 111
- 238000000926 separation method Methods 0.000 title claims abstract description 75
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 115
- 239000007789 gas Substances 0.000 claims abstract description 90
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 76
- 239000007788 liquid Substances 0.000 claims abstract description 73
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 55
- 238000005057 refrigeration Methods 0.000 claims abstract description 51
- 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
- 239000001257 hydrogen Substances 0.000 claims abstract description 28
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 28
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 24
- 239000003507 refrigerant Substances 0.000 claims abstract description 24
- 239000000203 mixture Substances 0.000 claims abstract description 16
- 238000000746 purification Methods 0.000 claims abstract description 12
- 239000003034 coal gas Substances 0.000 claims description 148
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 36
- 238000000034 method Methods 0.000 claims description 35
- 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 26
- 239000007791 liquid phase Substances 0.000 claims description 21
- 239000003245 coal Substances 0.000 claims description 20
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 20
- 229910052753 mercury Inorganic materials 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 229910021529 ammonia Inorganic materials 0.000 claims description 18
- 230000006835 compression Effects 0.000 claims description 18
- 238000007906 compression Methods 0.000 claims description 18
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 16
- 239000012071 phase Substances 0.000 claims description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 13
- 125000001741 organic sulfur group Chemical group 0.000 claims description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 12
- 229910052717 sulfur Inorganic materials 0.000 claims description 12
- 239000011593 sulfur Substances 0.000 claims description 12
- 238000010521 absorption reaction Methods 0.000 claims description 11
- 239000002253 acid Substances 0.000 claims description 11
- 238000005194 fractionation Methods 0.000 claims description 11
- 238000005406 washing Methods 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 239000011280 coal tar Substances 0.000 claims description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 9
- 239000007792 gaseous phase Substances 0.000 claims description 9
- 239000010687 lubricating oil Substances 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 7
- 230000008859 change Effects 0.000 claims description 7
- 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
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 6
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 6
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 239000011269 tar Substances 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 238000011068 loading method Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 2
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 claims 2
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims 2
- 239000000047 product Substances 0.000 description 29
- 239000003949 liquefied natural gas Substances 0.000 description 12
- 239000003463 adsorbent Substances 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 7
- 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
- 230000008569 process Effects 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 6
- 239000000470 constituent Substances 0.000 description 5
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 229960004424 carbon dioxide Drugs 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 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
- 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
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization 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
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 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
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 229940043237 diethanolamine Drugs 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- PCHPORCSPXIHLZ-UHFFFAOYSA-N diphenhydramine hydrochloride Chemical compound [Cl-].C=1C=CC=CC=1C(OCC[NH+](C)C)C1=CC=CC=C1 PCHPORCSPXIHLZ-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 235000003642 hunger Nutrition 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
- 239000000463 material Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 150000002790 naphthalenes Chemical class 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 210000000582 semen Anatomy 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, more particularly to a kind of gas fractionation unit for being pyrolyzed coal gas and gas separation side
Method.
Background technology
The resources supplIes of " rich coal, few gas, oil starvation ", determine that energy structure in China will be for a long time based on coal.Modern coalification
Work is an important channel for promoting Coal Clean Efficient Conversion to utilize, and the scientific and technical innovation and technology carried out around coal chemical industry is opened
Hair, there is considerable social effect and economic implications.It is coal chemical industry to be utilized with the leading coal sub-prime of pulverized coal pyrolysis technology
One of important technology path of industry.
Coal sub-prime takes out volatile ingredient (coal tar therein using referring to coal being pyrolyzed by middle low temperature distillation
Oil, coal gas), a kind of technique that remaining semicoke recycles.The pyrolysis coal gas active ingredient of the process by-product is high, wherein, methane contains
For amount more than 40%, hydrogen-rich Gas content reaches 14% more than 20%, C2~C5 contents.
Pyrolysis coal gas is such as directly used as fuel, and its value can not make full use of, and economy is poor.Therefore, it is necessary to by heat
Each useful constituent in solution coal gas is separated, and is realized making full use of for resource, is reduced the pollution to environment.
The content of the invention
In consideration of it, it is necessary to provide a kind of gas fractionation unit and gas separating method for being pyrolyzed coal gas.
A kind of gas fractionation unit for being pyrolyzed coal gas, including purifier and liquefaction separator；
The purifier is used to purify the pyrolysis coal gas；
The liquefaction separator include First Heat Exchanger, the first gas-liquid separator, mixed hydrocarbon rectifying column, the second heat exchanger,
Dehydrogenation rectifying column and methane rectifier column, the first entrance of the First Heat Exchanger are used to inputting the pyrolysis coal gas, and described first
The first outlet of heat exchanger connects with the entrance of first gas-liquid separator, the gaseous phase outlet of first gas-liquid separator and
The entrance connection of the mixed hydrocarbon rectifying column, the first mixed hydrocarbon product of liquid-phase outlet output of first gas-liquid separator are described mixed
The gaseous phase outlet of hydrocarbon rectifying column connects with the first entrance of second heat exchanger, the first outlet of second heat exchanger and institute
State the entrance connection of dehydrogenation rectifying column, the second mixed hydrocarbon product of liquid-phase outlet output of the mixed hydrocarbon rectifying column, the dehydrogenation rectifying
The gas vent of tower connects with the second entrance of second heat exchanger, the second outlet of second heat exchanger and described first
The second entrance connection of heat exchanger, the second outlet output hydrogen rich gas of the First Heat Exchanger, the liquid of the dehydrogenation rectifying column
Outlet connects with the entrance of the methane rectifier column, the liquid outlet output LNG product of the methane rectifier column, the methane essence
The gaseous phase outlet for evaporating tower connects with the 3rd entrance of second heat exchanger, the 3rd outlet of second heat exchanger and described the
The 3rd entrance connection of one heat exchanger, the 3rd outlet output tail gas of the First Heat Exchanger；
The liquefaction separator also includes mixed-refrigerant cycle refrigeration plant and nitrogen circulation refrigeration plant, described mixed
Refrigerant circulation refrigeration plant is closed to be used to provide cold, and the tower top for the mixed hydrocarbon rectifying column for the pyrolyzing coal gas liquefaction
Condenser provides cold, and the nitrogen circulation refrigeration plant is used for overhead condenser and the methane for the dehydrogenation rectifying column
The overhead condenser of rectifying column provides cold.
In one of the embodiments, the purifier includes the first compression set, degreasing unit, the water being sequentially communicated
Cleaning device, pretreatment unit, the second compression set, hydrolysis device, mercury removal device, deacidifying device and drying device；
First compression set is used to the pyrolyzing coal air pressure being reduced to 0.5MPa~0.8MPa；
The degreasing unit is used to remove the lubricating oil and coal tar in the pyrolysis coal gas；
The water washing device is used to remove the ammonia in the pyrolysis coal gas；
The pretreatment unit is used to remove the benzene and naphthalene in the pyrolysis coal gas；
Second compression set is used to continue to be compressed to 2MPa~4MPa by the pyrolysis coal gas；
It is inorganic sulfur that the hydrolysis device, which is used for the organic sulfur conversion in the pyrolysis coal gas,；
The mercury removal device is used to remove the mercury impurities in the pyrolysis coal gas；
The deacidifying device is used to remove the acid impurities in the pyrolysis coal gas；
The drying device is used to remove the water in the pyrolysis coal gas.
In one of the embodiments, the mixed-refrigerant cycle refrigeration plant includes the hybrid refrigeration pressure being sequentially communicated
Contracting machine, cooler and the second gas-liquid separator, the liquid outlet of second gas-liquid separator and the of the First Heat Exchanger
Four entrances connect, and the 4th outlet of the First Heat Exchanger connects with the 5th entrance of the First Heat Exchanger, and described first changes
Hot device the 5th outlet connect to form loop with the hybrid refrigeration compressor, the gas vent of second gas-liquid separator with
The 6th entrance connection of the First Heat Exchanger, the 6th outlet of the First Heat Exchanger and the 4th of second heat exchanger enter
Mouth connection, the 4th outlet of second heat exchanger connect with the 5th entrance of second heat exchanger, second heat exchanger
The 5th outlet connect with the 5th entrance of the First Heat Exchanger, the First Heat Exchanger the 5th outlet and it is described mix system
Cold compressor connects to form loop.
In one of the embodiments, the nitrogen circulation refrigeration plant includes nitrogen compressor, the nitrogen compressor
Outlet connected with the 7th entrance of the First Heat Exchanger, the First Heat Exchanger the 7th outlet and second heat exchanger
The 6th entrance connection, second heat exchanger the 6th outlet connected with the entrance of current divider, the first of the current divider goes out
Mouth connects with the nitrogen inlet of the overhead condenser of the dehydrogenation rectifying column, the nitrogen of the overhead condenser of the dehydrogenation rectifying column
Outlet connects with the first entrance of the second current collector, the overhead condensation of the second outlet of the current divider and the methane rectifier column
The second of the nitrogen inlet connection of device, the nitrogen outlet of the overhead condenser of the methane rectifier column and second current collector enters
Mouthful connection, the outlet of second current collector connects with the 7th entrance of second heat exchanger, and the of second heat exchanger
Seven outlets connect with the 8th entrance of the First Heat Exchanger, the 8th outlet of the First Heat Exchanger and the nitrogen compressor
Entrance connect to form loop.
A kind of gas separating method for being pyrolyzed coal gas, comprises the following steps：
Purify the pyrolysis coal gas；
Gas-liquid separation is carried out after pyrolysis coal gas after purification is cooled into -5 DEG C~-25 DEG C, output gas-liquid separation obtains
Liquid phase, obtain the first mixed hydrocarbon product；
The gas phase that gas-liquid separation is obtained carries out first time rectifying separation, exports the isolated liquid phase of first time rectifying,
Obtain the second mixed hydrocarbon product；
The isolated gas phase of first time rectifying is cooled to -145 DEG C~-165 DEG C, then, carries out second of rectifying point
From will be exported after the isolated gas heating of second of rectifying, obtain hydrogen rich gas；
The isolated liquid of second of rectifying is subjected to third time rectifying separation, the liquid of output third time rectifying separation
Body, LNG product is obtained, will be exported after the isolated tail gas heating of third time rectifying；
Wherein, use mix refrigerant to provide cold for the pyrolyzing coal gas liquefaction and first time rectifying separation, adopt
It is the offer cold that second of rectifying separation separates with the third time rectifying with nitrogen.
In one of the embodiments, the operation for purifying the pyrolysis coal gas comprises the following steps：
The pyrolyzing coal air pressure is reduced to 0.5MPa~0.8MPa；
Remove the lubricating oil and coal tar in the pyrolysis coal gas；
Remove the ammonia in the pyrolysis coal gas；
Remove the benzene and naphthalene in the pyrolysis coal gas；
The pyrolysis coal gas is continued to be compressed to 2MPa~4MPa；
It is inorganic sulfur by the organic sulfur conversion in the pyrolysis coal gas；
Remove the mercury impurities in the pyrolysis coal gas；
Remove the acid impurities in the pyrolysis coal gas；
Remove the water in the pyrolysis coal gas.
In one of the embodiments, in the operation for removing the ammonia in the pyrolysis coal gas, removed using the method for washing
Ammonia in the pyrolysis coal gas；
In the operation for removing the mercury impurities in the pyrolysis coal gas, using in the sulfur loading active carbon absorption pyrolysis coal gas
Mercury impurities.
In one of the embodiments, mix refrigerant is used as the pyrolyzing coal gas liquefaction and the first time rectifying point
From provide cold operation be：
After the mix refrigerant supercharging of low pressure, gas-liquid separation is carried out after being cooled to 40 DEG C, the liquid phase section after gas-liquid separation
After stream refrigeration, backflow and provide rewarming after cold for the pyrolyzing coal gas liquefaction, after the gas phase throttling refrigeration after gas-liquid separation, then
Backflow and provide cold for first time rectifying separation, after the pyrolyzing coal gas liquefaction offer cold is provided with the liquid phase backflowed
Rewarming, backflow to form loop.
In one of the embodiments, use nitrogen to separate with the third time rectifying for second of rectifying separation to carry
The operation of semen donors is：
40 DEG C are cooled to after nitrogen is compressed, after throttling refrigeration, for second of rectifying separation and the described 3rd
Secondary rectifying separation provides cold, and then backflow rewarming, forms loop.
In one of the embodiments, methane, hydrogen, C2, more than C2 components, and an oxygen are contained in the pyrolysis coal gas
Change one kind in the components such as carbon, nitrogen, carbon dioxide, organic sulfur, sulfur dioxide, hydrogen sulfide, ammonia, tar, dust and vapor
Or it is several, wherein, the volume content of methane is 40%~45%, and the volume content of hydrogen is 20%~25%, C2~C5 body
Product content is 10%~14%.
The gas fractionation unit and method of above-mentioned pyrolysis coal gas, after being pyrolyzed gas purification by purifier, then pass through
First gas-liquid separator carries out gas-liquid separation, and mixed hydrocarbon product, hydrogen rich gas and LNG can be obtained then through the separation of rectifying three times
Product, appliance arrangement is uncomplicated, and annexation is simple, and gas separating technology is simple, easily operation.
Brief description of the drawings
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.
Embodiment
In order that the objects, technical solutions and advantages of the present invention become apparent from, below in conjunction with drawings and Examples, to this hair
It is bright to be further elaborated.It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, and do not have to
It is of the invention in limiting.
Referring to Fig. 1, the gas fractionation unit of the pyrolysis coal gas of an embodiment, including purifier (not shown) and liquid
Change separator 100.
Purifier is used to purify pyrolysis coal gas.Be pyrolyzed coal gas in active principle methane volume content about 40%~
45%, volume content about 20%~25%, C2~C5 of hydrogen rich gas volume content about 10%~14%, also containing a small amount of one
The inert gases such as carbonoxide, nitrogen and carbon dioxide, micro organic sulfur, sulfur dioxide, hydrogen sulfide, ammonia, tar, dust and
One or more of impurity in vapor 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
100000Nm3/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 |
| It is total | 100 |
| Tar and dust | 1.43mg/Nm3 |
| Vapor | Saturation |
Purifier include be sequentially communicated the first compression set, degreasing unit, water washing device, pretreatment unit, second
Compression set, hydrolysis device, mercury removal device, deacidifying device and drying device.
First compression set is used to pyrolyzing coal air pressure being reduced to 0.5MPa~0.8MPa.First compression set can be screw rod
Compressor.
Degreasing unit is used to remove the lubricating oil and coal tar in pyrolysis coal gas.In the present embodiment, it can use and inhale
Attached method removes the lubricating oil and coal tar in pyrolysis coal gas.Adsorbent is one kind of activated carbon.The adsorbent can be with coal-based carbon
It is made for raw material, send coal-burning boiler to use after adsorption saturation.
Water washing device is used to remove the ammonia in pyrolysis coal gas.Water washing device can be water scrubber.Removed using the method for washing
The ammonia being pyrolyzed in coal gas is removed, ammonium salt crystallization can be avoided to influence plant running.
Pretreatment unit is used to remove the benzene and naphthalene in pyrolysis coal gas.In the present embodiment, can be taken off using absorption method
Except heavy constituent impurity such as the benzene in pyrolysis coal gas and naphthalenes.Adsorbent is used with good adsorption selectivity and larger adsorption capacity
Special adsorbent, high temperature regeneration after adsorption saturation, it is possible to achieve adsorbent recycles.The Special adsorbent can be activity
One kind of charcoal.
Second compression set is used to continue to be compressed to 2MPa~4MPa by pyrolysis coal gas.Second compression set can be reciprocal
Formula or centrifugal compressor.
It is inorganic sulfur that hydrolysis device, which is used for the organic sulfur conversion being pyrolyzed in coal gas,.In the present embodiment, can use
The organic sulfur conversion being pyrolyzed in coal gas is inorganic sulfur by medium temperature hydrolyzation technique.
Mercury removal device is used to remove the mercury impurities in pyrolysis coal gas.In the present embodiment, sulfur loading active carbon can be used
Micro mercury impurities in absorption pyrolysis coal gas.
Deacidifying device is used to remove the acid impurities in pyrolysis coal gas.In the present embodiment, chemical absorbing can be used
H in method removing pyrolysis coal gas2S、CO2Deng acid impurities.Absorbent is from MDEA (the N- methyl diethyls using piperazine as activator
Hydramine) solution.To ensure removal effect, the absorption and regeneration device of two sets of series connection is set.After depickling, the H in pyrolysis coal gas2S、CO2
It is less than 20ppm Deng acid impurities content.
Drying device is used to remove the water in pyrolysis coal gas.
In the present embodiment, dry absorbing process using molecular sieve is isobaric, pyrolysis dew point of gas after drying less than-
70℃。
Liquefaction separator 100 includes First Heat Exchanger 10, the first gas-liquid separator 20, mixed hydrocarbon rectifying column 30, second and changed
Hot device 40, dehydrogenation rectifying column 50 and methane rectifier column 60.
The first entrance of First Heat Exchanger 10 is used to input pyrolysis coal gas.Representative input pyrolysis coal gas at arrow 1 in Fig. 1.
The first outlet of First Heat Exchanger 10 connects with the entrance of the first gas-liquid separator 20.First Heat Exchanger 10 can change for plate-fin
Hot device.
The gaseous phase outlet of first gas-liquid separator 20 connects with the entrance of mixed hydrocarbon rectifying column 30.First gas-liquid separator 20
The first mixed hydrocarbon product of liquid-phase outlet output.First mixed hydrocarbon product is based on C5+ components and the mixed hydrocarbon product containing a small amount of light component.
The first mixed hydrocarbon product of representative output at arrow 2 in Fig. 1.
The first entrance connection of the gaseous phase outlet and the second heat exchanger 40 of mixed hydrocarbon rectifying column 30, the of the second heat exchanger 40
One outlet connects with the entrance of dehydrogenation rectifying column 50, mixes the second mixed hydrocarbon product of liquid-phase outlet output of hydrocarbon rectifying column 30.Second is mixed
Hydrocarbon product is based on C3, C4 component and the mixed hydrocarbon product containing a small amount of C2 and C5+.The second mixed hydrocarbon of representative output at arrow 3 in Fig. 1
Product.
The second entrance of the gas vent of dehydrogenation rectifying column 50 and the second heat exchanger 40 connects, and the of the second heat exchanger 40
Two outlets connect with the second entrance of First Heat Exchanger 10, the second outlet output hydrogen rich gas of First Heat Exchanger 10.Arrow in Fig. 1
Representative exports hydrogen rich gas at 4.Second heat exchanger 40 can be plate-fin heat exchanger.
The liquid outlet of dehydrogenation rectifying column 50 connects with the entrance of methane rectifier column 60.The liquid discharge of methane rectifier column 60
Mouth output LNG (Liquefied Natural Gas, liquefied natural gas) product.LNG product is sent to storage tank.In Fig. 1 at arrow 5
Represent output LNG product.
3rd entrance of the gaseous phase outlet of methane rectifier column 60 and the second heat exchanger 40 connects, and the of the second heat exchanger 40
Three outlets connect with the 3rd entrance of First Heat Exchanger 10, the 3rd outlet output tail gas of First Heat Exchanger 10.Tail gas is with an oxygen
Change based on carbon, and contain a small amount of hydrogen, nitrogen and trace methane.Representative exports tail gas at arrow 6 in Fig. 1.
Liquefaction separator 100 also includes mixed-refrigerant cycle refrigeration plant 70 and nitrogen circulation refrigeration plant 80.It is mixed
Refrigerant circulation refrigeration plant 70 is closed to be used to provide cold, and the overhead condensation for mixed hydrocarbon rectifying column 30 for pyrolyzing coal gas liquefaction
Device provides cold.Nitrogen circulation refrigeration plant 80 is used for overhead condenser 52 and methane rectifier column 60 for dehydrogenation rectifying column 50
Overhead condenser 62 provide cold.
In the present embodiment, mixed-refrigerant cycle refrigeration plant 70 includes the hybrid refrigeration compressor being sequentially communicated
72nd, the gas-liquid separator 76 of cooler 74 and second.Cooler 74 is aftercooler.It is additionally provided with before the entrance of refrigeration compressor 72 slow
Rush tank (not shown).
The liquid outlet of second gas-liquid separator 76 connects with the 4th entrance of First Heat Exchanger 10, First Heat Exchanger 10
4th outlet connects with the 5th entrance of First Heat Exchanger 10, the 5th outlet of First Heat Exchanger 10 and hybrid refrigeration compressor 72
Connection forms loop.Liquid phase after gas-liquid separation cools by First Heat Exchanger 10, then through the throttling refrigeration of first throttle valve 73
Afterwards, then backflow from the 5th entrance of First Heat Exchanger 10 and rewarming after cold is provided for pyrolyzing coal gas liquefaction, from First Heat Exchanger
After 10 the 5th outlet outflow, surge tank is flowed into, then flows into hybrid refrigeration compressor 72, forms loop.
The gas vent of second gas-liquid separator 76 connects with the 6th entrance of First Heat Exchanger 10, First Heat Exchanger 10
6th outlet connect with the 4th entrance of the second heat exchanger 40, and the 4th of the second heat exchanger 40 the exports the with the second heat exchanger 40
Five entrances connect, and the 5th outlet of the second heat exchanger 40 connects with the 5th entrance of First Heat Exchanger 10, First Heat Exchanger 10
5th outlet connects to form loop with hybrid refrigeration compressor 72.Gas phase after gas-liquid separation, pass sequentially through First Heat Exchanger 10,
After the cooling of second heat exchanger 40, then through the throttling refrigeration of second throttle 75, then backflowed from the 5th entrance of the second heat exchanger 40
Cold is provided to mix the overhead condenser of hydrocarbon rectifying column 30, after the 5th outlet outflow of the second heat exchanger 40, with the liquid to backflow
Enter First Heat Exchanger 10 from the 5th entrance of First Heat Exchanger 10 after mixing and rewarming after cold be provided for pyrolyzing coal gas liquefaction,
Again after the 5th outlet outflow of First Heat Exchanger 10, surge tank is flowed into, then flows into hybrid refrigeration compressor 72, forms loop.
Specifically, the gas phase backflowed of the 5th outlet outflow of the second heat exchanger 40 and the liquid phase backflowed mix at the first current collector 78
Convergence.
Nitrogen circulation refrigeration plant 80 includes nitrogen compressor 82.Nitrogen buffering is additionally provided with before the entrance of nitrogen compressor 82
Tank.The outlet of nitrogen compressor 82 is additionally provided with water cooler 84.The outlet of nitrogen compressor 82 and the 7th of First Heat Exchanger 10 enter
Mouth connection.Specifically, the outlet of nitrogen compressor 82 is connected by water cooler 84 with the 7th entrance of First Heat Exchanger 10.The
7th outlet of one heat exchanger 10 connects with the 6th entrance of the second heat exchanger 40.The 6th of second heat exchanger 40 exports and divided
Flow the nitrogen inlet company of the entrance connection of device 90, the first outlet of current divider 90 and the overhead condenser 52 of dehydrogenation rectifying column 50
It is logical, the first entrance connection of the nitrogen outlet of the overhead condenser 52 of dehydrogenation rectifying column 50 and the second current collector 95.Current divider 90
Second outlet connected with the nitrogen inlet of the overhead condenser 62 of methane rectifier column 60.The overhead condensation of methane rectifier column 60
The second entrance of the nitrogen outlet of device 62 and the second current collector 95 connects.The outlet of second current collector 95 and the second heat exchanger 40
The 7th entrance connection, the second heat exchanger 40 the 7th outlet connected with the 8th entrance of First Heat Exchanger 10, First Heat Exchanger
80 the 8th outlet connects to form loop with the entrance of nitrogen compressor 82.40 DEG C are cooled to after nitrogen is compressed, is passed sequentially through
The heat exchanger 40 of First Heat Exchanger 10 and second cools, then by the throttling refrigeration of the 3rd choke valve 86, is then divided by current divider 90
Into two strands, respectively the overhead condenser 62 of the overhead condenser 52 of dehydrogenation rectifying column 50 and methane rectifier column 60 provides cold,
Then the second heat exchanger 40 and the rewarming of First Heat Exchanger 10 are returned again to, nitrogen compressor 82 is then flowed into and forms loop.
The gas fractionation unit of above-mentioned pyrolysis coal gas, after being pyrolyzed gas purification by purifier, then by the first gas
Liquid/gas separator carries out gas-liquid separation, and mixed hydrocarbon product, hydrogen rich gas and LNG product can be obtained then through the separation of rectifying three times,
Appliance arrangement is uncomplicated, and annexation is simple, and gas separating technology is simple, easily operation.
In addition, also provide the gas separation side that a kind of gas fractionation unit using above-mentioned pyrolysis coal gas be pyrolyzed coal gas
Method.
Fig. 2 is refer to, in one embodiment, the gas separating method of coal gas is pyrolyzed, comprises the following steps：
S10, purification pyrolysis coal gas.
Fig. 3 is refer to, 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 S110, pyrolyzing coal air pressure is reduced to by 0.5MPa~0.8MPa using the first compression set.First compression set can
Think helical-lobe compressor.
S120, remove the lubricating oil and coal tar being pyrolyzed in coal gas.
The lubricating oil and coal tar in pyrolysis coal gas are removed using degreasing unit in S120.In the present embodiment, use
Absorption method removes the lubricating oil and coal tar in pyrolysis coal gas.Adsorbent is activated carbon, is made by raw material of coal-based carbon, and absorption is full
Coal-burning boiler is sent to use with after.
S130, remove the ammonia being pyrolyzed in coal gas.
In S130, the ammonia in pyrolysis coal gas is removed using water washing device.Removed using the method for washing in pyrolysis coal gas
Ammonia, ammonium salt crystallization can be avoided to influence plant running.
S140, remove the benzene and naphthalene being pyrolyzed in coal gas.
In S140, the benzene and naphthalene in pyrolysis coal gas are removed using pretreatment unit.In the present embodiment, it can use and inhale
The heavy constituent impurity such as benzene and naphthalene in attached method removing pyrolysis coal gas.Adsorbent, which uses, has good adsorption selectivity and larger absorption
The Special adsorbent of capacity, high temperature regeneration after adsorption saturation, it is possible to achieve adsorbent recycles.The Special adsorbent can be with
For one kind of activated carbon.
S150, will pyrolysis coal gas continue to be compressed to 2MPa~4MPa.
In S150, continue to be compressed to 2MPa~4MPa by coal gas is pyrolyzed using the second compression set.Second compression set can
Think reciprocating or centrifugal compressor.
S160, by be pyrolyzed coal gas in organic sulfur conversion be inorganic sulfur.
In S160, use hydrolysis device by the organic sulfur conversion being pyrolyzed in coal gas for inorganic sulfur.In the present embodiment, may be used
To use medium temperature hydrolyzation technique by the organic sulfur conversion being pyrolyzed in coal gas as inorganic sulfur.
S170, remove the mercury impurities being pyrolyzed in coal gas.
In S170, the mercury impurities in pyrolysis coal gas are removed using mercury removal device.In the present embodiment, it can use and carry sulphur
Micro mercury impurities in charcoal absorption pyrolysis coal gas.
S180, remove the acid impurities being pyrolyzed in coal gas.
In S180, the acid impurities in pyrolysis coal gas are removed using deacidifying device.In the present embodiment, it can use and change
Learn the H in absorption process removing pyrolysis coal gas2S、CO2Deng acid impurities.Absorbent is from MDEA (the N- first using piperazine as activator
Base diethanol amine) solution.To ensure removal effect, the absorption and regeneration device of two sets of series connection is set.After depickling, it is pyrolyzed in coal gas
H2S、CO2It is less than 20ppm Deng acid impurities content.
S190, remove the water being pyrolyzed in coal gas.
In S190, the water in pyrolysis coal gas is removed using drying device.
S20, gas-liquid separation is carried out after the pyrolysis coal gas after purification is cooled into -5 DEG C~-25 DEG C, output gas-liquid separation obtains
The liquid phase arrived, obtain the first mixed hydrocarbon product.
In S20, -5 DEG C~-25 DEG C are cooled to using First Heat Exchanger 10.It is pyrolyzing coal gas liquefaction by mix refrigerant
Cold is provided.Gas-liquid separation is carried out using gas-liquid separator 20.
S30, the gas phase for obtaining gas-liquid separation carry out first time rectifying separation, the isolated liquid of output first time rectifying
Phase, obtain the second mixed hydrocarbon product.
In S30, first time rectifying separation is carried out using mixed hydrocarbon rectifying column 30.
S40, the isolated gas phase of first time rectifying is cooled to -145 DEG C~-165 DEG C, then, carries out second of essence
Cut after the isolated gas heating of second of rectifying from will export, obtain hydrogen rich gas.
In S40, the isolated gas phase of first time rectifying is cooled to -145 DEG C~-165 DEG C using the second heat exchanger 40.
Second of rectifying separation is carried out using dehydrogenation rectifying column 50.Successively will be second using the second heat exchanger 40 and First Heat Exchanger 10
The isolated hydrogen rich gas heating of rectifying.Wherein, nitrogen gas refrigerant is used to provide cold for second of rectifying separation.
S50, the isolated liquid of second of rectifying is carried out to third time rectifying separation, the rectifying separation of output third time
Liquid, LNG product is obtained, will be exported after the isolated tail gas heating of third time rectifying.
In S50, third time rectifying separation is carried out using methane rectifier column 60.Using the second heat exchanger 40 and First Heat Exchanger
10 successively heat up the isolated tail gas of third time rectifying.Wherein, nitrogen gas refrigerant is used to be provided for third time rectifying separation
Cold.
Further, mix refrigerant is used to provide the operation stream of cold for pyrolyzing coal gas liquefaction and first time rectifying separation
Journey is as follows：
After the mix refrigerant supercharging of low pressure, gas-liquid separation is carried out after being cooled to 40 DEG C, the liquid phase section after gas-liquid separation
After stream refrigeration, backflow and provide rewarming after cold for pyrolyzing coal gas liquefaction, after the gas phase throttling refrigeration after gas-liquid separation, then backflow
Cold is provided for first time rectifying separation, pyrolyzing coal gas liquefaction is mixed into the liquid phase backflowed rewarming after cold, shape of backflowing is provided
Into loop.
Specifically, the mix refrigerant of low pressure is pressurized by hybrid refrigeration compressor 72.40 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, cooled by First Heat Exchanger 10, then
Throttled by first throttle valve 73, then flow back into First Heat Exchanger 10 with after pyrolysis coal gas progress heat exchange, rewarming flows out first
Heat exchanger 10, flow into the surge tank of the entrance of hybrid refrigeration compressor 72.Gas phase after gas-liquid separation, pass sequentially through the first heat exchange
The heat exchanger 40 of device 10 and second cools, then by the throttling refrigeration of second throttle 75, then flows back into the second heat exchanger 40 and
The isolated hydrogen rich gas of rectifying carries out heat exchange heating, and flows into First Heat Exchanger 10, stream after the liquid phase mixing backflowed
Enter surge tank.
Further, nitrogen is used to provide the operating process of cold such as second of rectifying separation and third time rectifying separation
Under：
Nitrogen is compressed or be cooled to 40 DEG C, the heat exchanger 40 of First Heat Exchanger 10 and second is passed sequentially through and cools, then pass through
After the throttling refrigeration of 3rd choke valve 86, cold then is provided for second of rectifying separation and third time rectifying separation, is then backflowed
Rewarming, form loop.
After nitrogen gas refrigerant first passes through low-pressure nitrogen surge tank, compressed by nitrogen compressor 82.Through water after pressure rise
Cooler 84 is cooled to 40 DEG C, cools successively by the heat exchanger 40 of First Heat Exchanger 10 and second, then saved by the 3rd choke valve 86
Stream refrigeration.Two strands, the respectively overhead condenser 52 and methane of dehydrogenation rectifying column 50 are divided into by current divider 90 after throttling refrigeration
The overhead condenser 62 of rectifying column 60 provides cold, then by the second current collector 95, returns again to the second heat exchanger 40 and first
The rewarming of heat exchanger 10, then flows into low-pressure nitrogen surge tank, and loop is formed into nitrogen compressor 82.
In the gas separating method of above-mentioned pyrolysis coal gas, it is combined using azeotrope circularly cooling and nitrogen circulation refrigeration
Refrigeration process, possess three advantages：First, energy consumption is relatively low；Second, equipment mature and reliable, manufacture craft is simple, and domestic equipment is
It can meet to require.By taking refrigeration compressor as an example, the separation of the cascade EDFA of no heavy constituent cryogen and complexity take out mouth, drop significantly
The manufacture requirement of low compressor, the simplification of operation and the stability of dynamic equipment operation are more favorable to, it is whole so as to ensure
The continuous and steady operation performance of kind of refrigeration cycle；Third, mix refrigerant is mainly by materials such as nitrogen, methane, ethene, propane, pentanes
Mix, select more reliable according to a certain percentage.
The gas separating method of above-mentioned pyrolysis coal gas, using a set of purification optimized and combined, cryogenic liquefying and cryogenic rectification
Physical separation process program, will be pyrolyzed coal gas in hydrogen, methane, ethane, ethene, propane, propylene, butane, butylene, pentane
Efficiently separated etc. component, produce the products such as hydrogen rich gas, LNG and mixed hydrocarbon respectively.The hydrogen rich gas in pyrolysis coal gas is isolated to be used to add
Hydrogen production device, LNG and mixed hydrocarbon are sold as product.By process optimization and the optimum choice of products scheme, by pyrolysis coal gas
Each useful constituent separation, obtained different product are used respectively, have expanded the industrial chain that coal sub-prime utilizes.With tradition profit
Compared with method, realize the rational and efficient use of resource, reduce the pollution to environment, while create considerable economic effect
Benefit.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 and resists more by force
The ability of the market risk.
Described above is only the preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
Member, 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 regarded as
Protection scope of the present invention.
Claims (8)
1. a kind of gas fractionation unit for being pyrolyzed coal gas, it is characterised in that including purifier and liquefaction separator；
The purifier is used to purify the pyrolysis coal gas；
The liquefaction separator includes First Heat Exchanger, the first gas-liquid separator, mixed hydrocarbon rectifying column, the second heat exchanger, dehydrogenation
Rectifying column and methane rectifier column, the first entrance of the First Heat Exchanger are used to input the pyrolysis coal gas, first heat exchange
The first outlet of device connects with the entrance of first gas-liquid separator, the gaseous phase outlet of first gas-liquid separator and described
The entrance connection of mixed hydrocarbon rectifying column, the first mixed hydrocarbon product of liquid-phase outlet output of first gas-liquid separator, the mixed hydrocarbon essence
The gaseous phase outlet for evaporating tower connects with the first entrance of second heat exchanger, the first outlet of second heat exchanger and described de-
The entrance connection of hydrogen rectifying column, the second mixed hydrocarbon product of liquid-phase outlet output of the mixed hydrocarbon rectifying column, the dehydrogenation rectifying column
Gas vent connects with the second entrance of second heat exchanger, the second outlet of second heat exchanger and first heat exchange
The second entrance connection of device, the second outlet output hydrogen rich gas of the First Heat Exchanger, the liquid outlet of the dehydrogenation rectifying column
Connected with the entrance of the methane rectifier column, the liquid outlet output LNG product of the methane rectifier column, the methane rectifier column
Gaseous phase outlet connected with the 3rd entrance of second heat exchanger, the 3rd outlet of second heat exchanger and described first change
The 3rd entrance connection of hot device, the 3rd outlet output tail gas of the First Heat Exchanger；
The liquefaction separator also includes mixed-refrigerant cycle refrigeration plant and nitrogen circulation refrigeration plant, the mixing system
Refrigerant cycle refrigeration plant is used to provide cold, and the overhead condensation for the mixed hydrocarbon rectifying column for the pyrolyzing coal gas liquefaction
Device provides cold, and the nitrogen circulation refrigeration plant is used for overhead condenser and the methane rectifying for the dehydrogenation rectifying column
The overhead condenser of tower provides cold；
The purifier include be sequentially communicated the first compression set, degreasing unit, water washing device, pretreatment unit, second
Compression set, hydrolysis device, mercury removal device, deacidifying device and drying device；
First compression set is used to the pyrolyzing coal air pressure being reduced to 0.5MPa~0.8MPa；
The degreasing unit is used to remove the lubricating oil and coal tar in the pyrolysis coal gas；
The water washing device is used to remove the ammonia in the pyrolysis coal gas；
The pretreatment unit is used to remove the benzene and naphthalene in the pyrolysis coal gas；
Second compression set is used to continue to be compressed to 2MPa~4MPa by the pyrolysis coal gas；
It is inorganic sulfur that the hydrolysis device, which is used for the organic sulfur conversion in the pyrolysis coal gas,；
The mercury removal device is used to remove the mercury impurities in the pyrolysis coal gas；
The deacidifying device is used to remove the acid impurities in the pyrolysis coal gas；
The drying device is used to remove the water in the pyrolysis coal gas；
Contain methane, hydrogen and C2~C5, and carbon monoxide, nitrogen, carbon dioxide, organic sulfur, two in the pyrolysis coal gas
One or more in sulfur oxide, hydrogen sulfide, ammonia, tar, dust and vapor, wherein, the volume content of methane for 40%~
45%, the volume content that the volume content of hydrogen is 20%~25%, C2~C5 is 10%~14%.
2. the gas fractionation unit of pyrolysis coal gas as claimed in claim 1, it is characterised in that the mixed-refrigerant cycle system
Cool equipment includes hybrid refrigeration compressor, cooler and the second gas-liquid separator being sequentially communicated, second gas-liquid separator
Liquid outlet connected with the 4th entrance of the First Heat Exchanger, the 4th outlet of the First Heat Exchanger and described first change
The 5th entrance connection of hot device, the 5th outlet of the First Heat Exchanger connect to form loop with the hybrid refrigeration compressor,
The gas vent of second gas-liquid separator connects with the 6th entrance of the First Heat Exchanger, and the of the First Heat Exchanger
Six outlets connect with the 4th entrance of second heat exchanger, the 4th outlet of second heat exchanger and second heat exchanger
The connection of the 5th entrance, the 5th outlet of second heat exchanger connects with the 5th entrance of the First Heat Exchanger, described the
5th outlet of one heat exchanger connects to form loop with the hybrid refrigeration compressor.
3. the gas fractionation unit of pyrolysis coal gas as claimed in claim 1, it is characterised in that the nitrogen circulation refrigeration plant
Including nitrogen compressor, the outlet of the nitrogen compressor connects with the 7th entrance of the First Heat Exchanger, and described first changes
7th outlet of hot device connects with the 6th entrance of second heat exchanger, the 6th outlet of second heat exchanger and current divider
Entrance connection, the first outlet of the current divider connects with the nitrogen inlet of the overhead condenser of the dehydrogenation rectifying column, institute
The first entrance of the nitrogen outlet and the second current collector of stating the overhead condenser of dehydrogenation rectifying column connects, and the second of the current divider
Outlet connects with the nitrogen inlet of the overhead condenser of the methane rectifier column, the nitrogen of the overhead condenser of the methane rectifier column
Gas outlet connect with the second entrance of second current collector, and export with second heat exchanger the of second current collector
Seven entrances connect, and the 7th outlet of second heat exchanger connects with the 8th entrance of the First Heat Exchanger, and described first changes
8th outlet of hot device connects to form loop with the entrance of the nitrogen compressor.
4. a kind of gas separating method for being pyrolyzed coal gas, it is characterised in that comprise the following steps：
Purify the pyrolysis coal gas；
Gas-liquid separation is carried out after pyrolysis coal gas after purification is cooled into -5 DEG C~-25 DEG C, exports the liquid phase that gas-liquid separation obtains,
Obtain the first mixed hydrocarbon product；
The gas phase that gas-liquid separation is obtained carries out first time rectifying separation, the isolated liquid phase of output first time rectifying, obtains
Second mixed hydrocarbon product；
The isolated gas phase of first time rectifying is cooled to -145 DEG C~-165 DEG C, then, carries out second of rectifying separation, will
Exported after the isolated gas heating of second of rectifying, obtain hydrogen rich gas；
The isolated liquid of second of rectifying is subjected to third time rectifying separation, the liquid of output third time rectifying separation, obtained
To LNG product, will be exported after the isolated tail gas heating of third time rectifying；
Wherein, mix refrigerant is used to provide cold for the pyrolyzing coal gas liquefaction and first time rectifying separation, using nitrogen
Gas separates with the third time rectifying for second of rectifying separation and provides cold；
Contain methane, hydrogen and C2~C5, and carbon monoxide, nitrogen, carbon dioxide, organic sulfur, two in the pyrolysis coal gas
One or more in sulfur oxide, hydrogen sulfide, ammonia, tar, dust and vapor, wherein, the volume content of methane for 40%~
45%, the volume content that the volume content of hydrogen is 20%~25%, C2~C5 is 10%~14%.
5. the gas separating method of pyrolysis coal gas as claimed in claim 4, it is characterised in that the behaviour of the purification pyrolysis coal gas
Work comprises the following steps：
The pyrolyzing coal air pressure is reduced to 0.5MPa~0.8MPa；
Remove the lubricating oil and coal tar in the pyrolysis coal gas；
Remove the ammonia in the pyrolysis coal gas；
Remove the benzene and naphthalene in the pyrolysis coal gas；
The pyrolysis coal gas is continued to be compressed to 2MPa~4MPa；
It is inorganic sulfur by the organic sulfur conversion in the pyrolysis coal gas；
Remove the mercury impurities in the pyrolysis coal gas；
Remove the acid impurities in the pyrolysis coal gas；
Remove the water in the pyrolysis coal gas.
6. the gas separating method of pyrolysis coal gas as claimed in claim 5, it is characterised in that
In the operation for removing the ammonia in the pyrolysis coal gas, the ammonia in the pyrolysis coal gas is removed using the method for washing；
It is miscellaneous using the mercury in the sulfur loading active carbon absorption pyrolysis coal gas in the operation for removing the mercury impurities in the pyrolysis coal gas
Matter.
7. the gas separating method of pyrolysis coal gas as claimed in claim 4, it is characterised in that it is described to use mix refrigerant
Pyrolyzing coal gas liquefaction and the first time rectifying separation provide cold operation be：
After the mix refrigerant supercharging of low pressure, gas-liquid separation is carried out after being cooled to 40 DEG C, the liquid phase throttling system after gas-liquid separation
After cold, backflow and provide rewarming after cold for the pyrolyzing coal gas liquefaction, after the gas phase throttling refrigeration after gas-liquid separation, then backflow
Cold is provided for first time rectifying separation, is mixed into the liquid phase backflowed after the pyrolyzing coal gas liquefaction offer cold again
Temperature, backflow to form loop.
8. the gas separating method of pyrolysis coal gas as claimed in claim 4, it is characterised in that use nitrogen as described second
Rectifying separation separated with the third time rectifying offer cold operation be：
40 DEG C are cooled to after nitrogen is compressed, after throttling refrigeration, for second of rectifying separation and third time essence
Cut is from cold is provided, and then backflow rewarming, forms loop.
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| CN109099642A (en) * | 2018-09-17 | 2018-12-28 | 陕西黑猫焦化股份有限公司 | A kind of clean gas produces the method and device of LNG coproduction nitrogen hydrogen, richness CO |
| CN110387274B (en) * | 2019-07-20 | 2024-08-02 | 中科瑞奥能源科技股份有限公司 | Equipment and method for preparing LNG and coproducing LPG by pyrolyzing coal gas |
| 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 |
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| US3625016A (en) * | 1968-06-07 | 1971-12-07 | Mc Donnell Douglas Corp | Separation of hydrogen and hydrocarbon mixtures by plural stage distillation with heat exchange |
| US5983665A (en) * | 1998-03-03 | 1999-11-16 | Air Products And Chemicals, Inc. | Production of refrigerated liquid methane |
| CN101782308A (en) * | 2009-08-26 | 2010-07-21 | 成都蜀远煤基能源科技有限公司 | Heat exchange system for cryogenic separation device for coal gasification device feed gas methane |
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