CN103423969A - Method for optimizing ethylene device compression area and reducing outlet pressure of cracking furnace - Google Patents
Method for optimizing ethylene device compression area and reducing outlet pressure of cracking furnace Download PDFInfo
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- CN103423969A CN103423969A CN2013103855153A CN201310385515A CN103423969A CN 103423969 A CN103423969 A CN 103423969A CN 2013103855153 A CN2013103855153 A CN 2013103855153A CN 201310385515 A CN201310385515 A CN 201310385515A CN 103423969 A CN103423969 A CN 103423969A
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- 238000005336 cracking Methods 0.000 title claims abstract description 45
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 239000005977 Ethylene Substances 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000006835 compression Effects 0.000 title claims abstract description 9
- 238000007906 compression Methods 0.000 title claims abstract description 9
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 230000008569 process Effects 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 41
- 238000000926 separation method Methods 0.000 claims description 29
- 239000007791 liquid phase Substances 0.000 claims description 24
- 239000012071 phase Substances 0.000 claims description 24
- 239000000463 material Substances 0.000 claims description 23
- 238000000197 pyrolysis Methods 0.000 claims description 15
- 229930195733 hydrocarbon Natural products 0.000 claims description 13
- 150000002430 hydrocarbons Chemical class 0.000 claims description 13
- 239000004215 Carbon black (E152) Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 238000005457 optimization Methods 0.000 claims description 9
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 239000003518 caustics Substances 0.000 claims description 5
- 230000009467 reduction Effects 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 2
- 238000009833 condensation Methods 0.000 abstract description 5
- 230000005494 condensation Effects 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 76
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 206010013786 Dry skin Diseases 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000004078 cryogenic material Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- -1 propylene, butylene, butadiene Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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Abstract
The invention discloses a method for optimizing an ethylene device compression area and reducing the outlet pressure of a cracking furnace. In the method, the processing capacity of front three sections of a compressor is improved by connecting small compressors in sections I, II and III of the cracking gas compressor in parallel; internal circulation matter flows in sections IV and V of the compressor are reduced and the treatment capacity of the sections IV and V of the compressor is improved by optimizing the treatment process on condensation liquid between the sections IV and V of the cracking gas compressor; the treatment capacity of the compressor is improved, the capacity enlarging and yield increasing of an ethylene device can be realized, or the suction pressure of the section I of the compressor can be reduced under the condition of the same or basically unchanged ethylene yield, so the outlet pressure (COP) of the cracking furnace is correspondingly reduced and the yield of high-value-added products can be improved. The method is flexible to operate, one or more small compressors can be added, one or more certain sections of the compression area can be transformed, or the whole compression can be transformed.
Description
Technical field
The invention discloses a kind ofly for ethylene cracking gas compressional zone transformation, and reduce the method for pyrolysis furnace outlet pressure.
Technical background
Petro chemical industry has very important status in national economy and social development, and the development of petrochemical industry has promoted the huge advance made of national economy.Ethene, propylene, butylene, butadiene etc. are the most basic raw materials of petrochemical industry, ethylene unit is the most important process units of above raw material, the method of preparing ethylene has a lot, but the most ripe with the pyrolysis in tubular furnace technology, 99% left and right of world Ethylene output is all produced by the pyrolysis in tubular furnace method.Ethylene unit generally adopts the mode of cryogenic separation to reclaim alkene, before cryogenic separation, to be compressed cracking gas, can improve the operating temperature of cryogenic separation on the one hand, thereby save cryogenic energy and cryogenic material, pressurization can impel water and heavy hydrocarbon condensation in cracking on the other hand, can remove moisture and the heavy hydrocarbon of a great deal of, thereby reduce the burden that drying and dehydrating separates with rectifying.
The many employing orders of the ethylene unit of China separation process, the general scheme that adopts five sections compressions of cracking gas compression in the order separation process, intersegmental interpolation water cooler is provided with caustic wash tower, with sour gas such as carbon dioxide removal, hydrogen sulfide between three or four sections.The condensation hydro carbons of first three section of compressor is delivered to gasoline stripping tower, four sections condensation hydro carbons enter condensate stripper, the hydro carbons of five sections condensations is after the chilled water (chw) heating, in the flash tank flash distillation, the lime set of flash distillation does not enter condensate stripper yet, and the condensate stripper tower bottoms enters depropanizing tower, the light component of carbon below two steams and returns to four sections entrances of compressor, this strand of gas can circulate in compressor, has increased the power of compressor, reduces the disposal ability of compressor.
Since the 80s and 90s in last century, along with the lasting expansion of China's ethylene unit can be increased production and the impact of raw material lighting, the charge gas compressor of most ethylene units is all in the overload operation state, and the disposal ability of charge gas compressor, become the restriction ethylene unit and further expand the bottleneck that can increase production; And cracking reaction is the reaction that molecular number increases, low pressure is conducive to reaction carries out to positive direction, and research shows: reduce the cracking outlet pressure of furnace, can improve the yield of the high value added products such as ethene, propylene, butadiene.But reduce the pyrolysis furnace outlet pressure, can cause one section suction pressure of compressor to reduce, for reaching identical compression effectiveness, the load of charge gas compressor must increase, so the reduction of pyrolysis furnace outlet pressure is limited by the disposal ability of charge gas compressor.The present invention proposes a kind of method of Optimization of Ethylene device compressional zone and reduction pyrolysis furnace outlet pressure for this reason.
Summary of the invention
The invention discloses a kind of method of Optimization of Ethylene device compressional zone and reduction pyrolysis furnace outlet pressure, this method, by one section of charge gas compressor, two sections and three sections light duty compressors in parallel, improves the disposal ability of first three section of compressor; And, by optimizing the treatment process of four, five sections intersegmental lime sets of charge gas compressor, reduce compressor four, five intersegmental part recycle flows, improve the disposal ability of four, five sections, compressor; Improving the compressor disposal ability, is that ethylene unit expands the key that can increase production, and in the situation that output is constant or change little, can reduce by one section suction pressure of compressor, thereby reduce the pyrolysis furnace outlet pressure, increase the yield of high value added product, this method comprises following key step:
(1) cracking gas from the water scrubber tower top enters one section suction tank of charge gas compressor, gas-liquid separation, and at the bottom of tank, liquid phase is returned to water scrubber by pump; The tank deck gas phase is divided into two parts part and enters one section supercharging of charge gas compressor, and another part enters one supercharging of newly-increased light duty compressor, and the cracking gas after supercharging can import charge gas compressor one section outlet material, second stage exit material or three sections outlet materials;
Cracking gas after (2) one sections superchargings, after water cooler is cooling, enters two sections suction tank gas-liquid separations, liquid phase water-oil separating at the bottom of tank, and water returns to one section suction tank, and liquid hydrocarbon is delivered to gasoline stripping tower by pump; The tank deck gas phase is divided into two parts, and a part enters two sections superchargings of charge gas compressor, and another part enters two superchargings of newly-increased light duty compressor, and the cracking gas after supercharging can import charge gas compressor second stage exit material or three sections outlet materials;
Cracking gas after (3) two sections superchargings enters three sections suction tanks of compressor after water cooler is cooling, gas-liquid separation in three sections suction tanks, and at the bottom of tank, liquid phase is returned to two sections suction tanks; The tank deck gas phase is divided into two parts, and a part enters three sections superchargings of charge gas compressor, and another part enters three superchargings of newly-increased light duty compressor, and three sections outlet materials of the cracking gas after supercharging and charge gas compressor converge;
Cracking gas after (4) three sections superchargings enters three sections drain tanks of compressor after water cooler is cooling, gas-liquid separation in three sections drain tanks, and at the bottom of tank, liquid phase is returned to three sections suction tanks, and the tank deck gas phase enters the washing caustic wash tower, enters four sections suction tanks after removing sour gas; Cracking gas gas-liquid separation in four sections suction tanks, at the bottom of tank, liquid phase is returned to water scrubber, and the tank deck gas phase enters four sections superchargings of charge gas compressor;
Cracking gas after (5) four sections superchargings enters five sections suction tanks of compressor after water cooler is cooling, gas-liquid separation in five sections suction tanks, and the tank deck gas phase enters five sections of charge gas compressors, enters rear system after supercharging; Liquid phase water-oil separating at the bottom of tank, water returns to four sections suction tanks, and liquid hydrocarbon enters condensate stripper to be separated, and materials at bottom of tower enters depropanizing tower, and the tower top material enters the light duty compressor four newly added, and enters rear system after supercharging.
Compared with prior art, good effect of the present invention is:
(1) improved the disposal ability of charge gas compressor, for the expansion of ethylene unit, can increase production and eliminate bottleneck.
(2) reduce the cracking gas outlet pressure, improved the productive rate of high value added product.
(3) flexible operation is reliable, can be according to demand a certain section or several sections of compressional zone be optimized, and also can be optimized whole compressional zone.
(4) use lower helical-lobe compressor and the reciprocating compressor of price, improvement cost is lower, and device fabrication and construction and installation cycle are shorter.
The accompanying drawing explanation:
By example, the mode with reference to accompanying drawing illustrates in the present invention, wherein:
Fig. 1 is embodiment mono-schematic diagram
Fig. 2 is embodiment bis-schematic diagrames
The specific embodiment
Embodiment mono-
Cracking gas from water scrubber tower top 0.045MPa.g enters one section suction tank 1 of compressor, gas-liquid separation, at the bottom of tank, liquid phase is returned to water scrubber by pump, the tank deck gas phase is divided into two parts part and enters charge gas compressor and be pressurized to a 0.17MPa.g for 2, another part enters newly-increased compressor 3 and is pressurized to 0.17MPa.g, two strands of cracking gases after supercharging converge, and enter two sections suction tanks 5 of compressor after going to 38 ℃ through water cooler 4 is cold; Cracking gas gas-liquid separation in two sections suction tanks, liquid phase water-oil separating at the bottom of tank, water returns to one section suction tank, liquid hydrocarbon is delivered to gasoline stripping tower by pump, and the tank deck gas phase is divided into two parts, and a part enters charge gas compressor and is pressurized to 0.415MPa.g for two section 6, another part enters newly-increased compressor 27 and is pressurized to 0.415MPa.g, two strands of cracking gases after supercharging converge, and after water cooler 8 is cooled to 38 ℃, enter three sections suction tanks 9 of compressor; Cracking gas gas-liquid separation in three sections suction tanks, at the bottom of tank, liquid phase is returned to two sections suction tanks 5, the tank deck gas phase is divided into two parts, a part enters charge gas compressor and is pressurized to 0.920MPa.g for three section 10, another part enters newly-increased compressor 3 11 and is pressurized to 0.920MPa.g, two strands of cracking gases after supercharging converge, and after water cooler is cooled to 38 ℃, enter three sections drain tanks 13 of compressor;
Cracking gas gas-liquid separation in three sections drain tanks 13, at the bottom of tank, liquid phase is returned to three sections suction tanks 9, and the tank deck gas phase enters washing caustic wash tower 14, enters four sections suction tanks 15 after removing sour gas; Cracking gas gas-liquid separation in four sections suction tanks, at the bottom of tank, liquid phase is returned to water scrubber, and the tank deck gas phase enters charge gas compressor and is pressurized to 1.732MPa.g for four section 16, enters five sections suction tanks 18 of compressor after water cooler 17 is cooled to 38 ℃; Cracking gas after four sections superchargings is five sections interior gas-liquid separations of suction tank 18, and the tank deck gas phase enters five section 19 of charge gas compressor, is pressurized to after 3.7MPa.g to enter rear system and processed; Liquid phase water-oil separating at the bottom of tank, water returns to four sections suction tanks 15, and liquid hydrocarbon enters condensate stripper 21 to be separated, materials at bottom of tower enters depropanizing tower, the tower top material enters the compressor 4 22 newly added, and is pressurized to 3.7MPa.g, with five sections outlet materials of charge gas compressor, converges.
Embodiment bis-
Cracking gas from water scrubber tower top 0.045MPa.g enters one section suction tank 1 of compressor, gas-liquid separation, at the bottom of tank, liquid phase is returned to water scrubber by pump, the tank deck gas phase is divided into two parts part and enters charge gas compressor and be pressurized to a 0.17MPa.g for 2, another part enters newly-increased compressor 1 and is pressurized to 0.415MPa.g, after supercharging, with charge gas compressor second stage exit material, converges; Cracking gas after one section supercharging enters two sections suction tanks 5 of compressor after water cooler is cooled to 38 ℃, gas-liquid separation in two sections suction tanks, liquid phase water-oil separating at the bottom of tank, water returns to one section suction tank 1, liquid hydrocarbon is delivered to gasoline stripping tower by pump, the tank deck gas phase enters charge gas compressor and is pressurized to 0.415MPa.g for two section 6, after water cooler 7 is cooled to 38 ℃, enters three sections suction tanks 8 of compressor; Cracking gas is three sections interior gas-liquid separations of suction tank 8; at the bottom of tank, liquid phase is returned to two sections suction tanks 5; the tank deck gas phase is divided into two parts; a part enters charge gas compressor and is pressurized to 0.920MPa.g for three section 9; another part enters newly-increased compressor 3 10 and is pressurized to 0.920MPa.g; converge with three sections outlet logistics of charge gas compressor after supercharging, after water cooler 11 is cooled to 38 ℃, enter three sections drain tanks 12 of compressor;
Cracking gas gas-liquid separation in three sections drain tanks 12, at the bottom of tank, liquid phase is returned to three sections suction tanks 8, and the tank deck gas phase enters washing caustic wash tower 13, enters four sections suction tanks 14 after removing sour gas; Cracking gas gas-liquid separation in four sections suction tanks 14, at the bottom of tank, liquid phase is returned to water scrubber, and the tank deck gas phase enters charge gas compressor and is pressurized to 1.732MPa.g for four section 15, enters five sections suction tanks 17 of compressor after water cooler 16 is cooled to 38 ℃; Cracking gas is five sections interior gas-liquid separations of suction tank 17, and the tank deck gas phase enters five section 18 of charge gas compressor, is pressurized to after 3.7MPa.g to enter rear system and processed; Liquid phase water-oil separating at the bottom of tank, water returns to four sections suction tanks 14, liquid hydrocarbon enters condensate stripper 20 to be separated, and materials at bottom of tower enters depropanizing tower, and the tower top material enters the compressor 4 21 newly added, be pressurized to 0.85MPa.g, separate aqueous water through water distributing can 22, drying device 23 dryings, forecooler 24 is cold to be gone to 10 ℃, after advancing again ice chest 25 and being cooled to-60 ℃, enter domethanizing column.
Claims (7)
1. an Optimization of Ethylene device compressional zone and reduce the method for pyrolysis furnace outlet pressure, it is characterized in that: the disposal ability that improves charge gas compressor by Optimization of Ethylene device compressional zone, for expanding to increase production, ethylene unit eliminates bottleneck, and in the situation that output is identical or change little, reduce by one section suction pressure of compressor, thereby reduce the pyrolysis furnace outlet pressure, improve the yield of high value added product, comprise following key step:
(1) cracking gas from the water scrubber tower top enters one section suction tank of charge gas compressor, gas-liquid separation, and at the bottom of tank, liquid phase is returned to water scrubber by pump; The tank deck gas phase is divided into two parts part and enters one section supercharging of charge gas compressor, and another part enters one supercharging of newly-increased light duty compressor, and the cracking gas after supercharging can import charge gas compressor one section outlet material, second stage exit material or three sections outlet materials;
Cracking gas after (2) one sections superchargings, after water cooler is cooling, enters two sections suction tank gas-liquid separations, liquid phase water-oil separating at the bottom of tank, and water returns to one section suction tank, and liquid hydrocarbon is delivered to gasoline stripping tower by pump; The tank deck gas phase is divided into two parts, and a part enters two sections superchargings of charge gas compressor, and another part enters two superchargings of newly-increased light duty compressor, and the cracking gas after supercharging can import charge gas compressor second stage exit material or three sections outlet materials;
Cracking gas after (3) two sections superchargings enters three sections suction tanks of compressor after water cooler is cooling, gas-liquid separation in three sections suction tanks, and at the bottom of tank, liquid phase is returned to two sections suction tanks; The tank deck gas phase is divided into two parts, and a part enters three sections superchargings of charge gas compressor, and another part enters three superchargings of newly-increased light duty compressor, and three sections outlet materials of the cracking gas after supercharging and charge gas compressor converge;
Cracking gas after (4) three sections superchargings enters three sections drain tanks of compressor after water cooler is cooling, gas-liquid separation in three sections drain tanks, and at the bottom of tank, liquid phase is returned to three sections suction tanks, and the tank deck gas phase enters the washing caustic wash tower, enters four sections suction tanks after removing sour gas; Cracking gas gas-liquid separation in four sections suction tanks, at the bottom of tank, liquid phase is returned to water scrubber, and the tank deck gas phase enters four sections superchargings of charge gas compressor;
Cracking gas after (5) four sections superchargings enters five sections suction tanks of compressor after water cooler is cooling, gas-liquid separation in five sections suction tanks, and the tank deck gas phase enters five sections of charge gas compressors, enters rear system after supercharging; Liquid phase water-oil separating at the bottom of tank, water returns to four sections suction tanks, and liquid hydrocarbon enters condensate stripper to be separated, and materials at bottom of tower enters depropanizing tower, and the tower top material enters the light duty compressor four newly added, and after supercharging, material can return to compressional zone or enter after treatment domethanizing column.
2. the method for a kind of Optimization of Ethylene device compressional zone according to claim 1 and reduction pyrolysis furnace outlet pressure, is characterized in that: the light duty compressor that newly-increased light duty compressor type is screw compressor, reciprocating compressor or other types.
3. a kind of Optimization of Ethylene device compressional zone according to claim 1 and reduce the method for pyrolysis furnace outlet pressure, it is characterized in that: new compressor one, compressor two, compressor three and compressor four can configure separately, and certain part of compressional zone is optimized; Also can be as required many configurations simultaneously, a plurality of positions or the whole compressional zone of compressional zone is optimized.
4. a kind of Optimization of Ethylene device compressional zone according to claim 1 and reduce the method for pyrolysis furnace outlet pressure, it is characterized in that: compressed machine four compressions of condensate stripper overhead gas are pressurized to 3.2MPa.g～3.9MPa.g, converge with five sections outlet logistics of charge gas compressor, or enter five sections drain tanks after water-cooled.
5. a kind of Optimization of Ethylene device compressional zone according to claim 1 and reduce the method for pyrolysis furnace outlet pressure, it is characterized in that: compressed machine four compressions of condensate stripper overhead gas are pressurized to 0.78MPa.g～2.0MPa.g, after drying is cooling, enter domethanizing column.
6. condensate stripper overhead gas according to claim 5 enters the domethanizing column flow process, it is characterized in that: drier used and cooler can arrange separately also can rely on existing equipment.
7. condensate stripper overhead gas according to claim 5 enters the domethanizing column flow process, it is characterized in that: the temperature that the condensate stripper overhead stream enters domethanizing column is-50 ℃ ~-80 ℃.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| TWI572706B (en) * | 2015-05-29 | 2017-03-01 | Nat Univ Tsing Hua | Carbon five product separation device |
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