EP0036151A1 - Procédé de décokage de refroidisseurs de gaz craqués - Google Patents
Procédé de décokage de refroidisseurs de gaz craqués Download PDFInfo
- Publication number
- EP0036151A1 EP0036151A1 EP81101665A EP81101665A EP0036151A1 EP 0036151 A1 EP0036151 A1 EP 0036151A1 EP 81101665 A EP81101665 A EP 81101665A EP 81101665 A EP81101665 A EP 81101665A EP 0036151 A1 EP0036151 A1 EP 0036151A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- cracked gas
- gas cooler
- cracked
- air
- heated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000007789 gas Substances 0.000 title claims abstract description 143
- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000005235 decoking Methods 0.000 title claims abstract description 31
- 230000008569 process Effects 0.000 title claims abstract description 13
- 238000005336 cracking Methods 0.000 claims abstract description 72
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000000203 mixture Substances 0.000 claims abstract description 35
- 239000000571 coke Substances 0.000 claims abstract description 20
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 18
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 18
- 238000001816 cooling Methods 0.000 claims abstract description 14
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000005977 Ethylene Substances 0.000 claims abstract description 12
- 238000004227 thermal cracking Methods 0.000 claims abstract description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 238000009835 boiling Methods 0.000 claims description 9
- 238000004140 cleaning Methods 0.000 claims description 9
- 239000004215 Carbon black (E152) Substances 0.000 claims description 8
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 239000011874 heated mixture Substances 0.000 claims description 2
- 239000003502 gasoline Substances 0.000 description 8
- 239000003921 oil Substances 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000003350 kerosene Substances 0.000 description 3
- 239000000463 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
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- RXXCIBALSKQCAE-UHFFFAOYSA-N 3-methylbutoxymethylbenzene Chemical compound CC(C)CCOCC1=CC=CC=C1 RXXCIBALSKQCAE-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003779 heat-resistant material Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000001294 propane Substances 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
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000005488 sandblasting Methods 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000007669 thermal treatment Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000011179 visual inspection Methods 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B08—CLEANING
- B08B—CLEANING IN GENERAL; PREVENTION OF FOULING IN GENERAL
- B08B9/00—Cleaning hollow articles by methods or apparatus specially adapted thereto
- B08B9/02—Cleaning pipes or tubes or systems of pipes or tubes
- B08B9/027—Cleaning the internal surfaces; Removal of blockages
- B08B9/032—Cleaning the internal surfaces; Removal of blockages by the mechanical action of a moving fluid, e.g. by flushing
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/16—Preventing or removing incrustation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B08—CLEANING
- B08B—CLEANING IN GENERAL; PREVENTION OF FOULING IN GENERAL
- B08B2230/00—Other cleaning aspects applicable to all B08B range
- B08B2230/01—Cleaning with steam
Definitions
- the present invention relates to a method for thermal decoking of cracked gas coolers for indirect cooling by means of water of ethylene-containing cracked gases which are obtained by thermal cracking of hydrocarbons in the presence of steam in an indirectly heated tubular cracking furnace.
- Thermal cracking of hydrocarbons in the presence of water vapor in an indirectly heated tube cracking furnace is widely used in ethylene plants (steam crackers), in which, in addition to ethylene, there are other valuable unsaturated compounds such as propylene and butadiene as well as pyrolysis gasoline with a high proportion of aromatic hydrocarbons such as benzene , Toluene and xylene can be obtained.
- steam crackers in which, in addition to ethylene, there are other valuable unsaturated compounds such as propylene and butadiene as well as pyrolysis gasoline with a high proportion of aromatic hydrocarbons such as benzene , Toluene and xylene can be obtained.
- dwell times for the hydrocarbons in the cracked tubes of the tubular cracking furnace of 0.1 to 0.5 seconds and exit temperatures of the cracked gases from the cracked tubes of more than 750 ° C., generally between 800 and 900 ° C., are preferably observed .
- the cracked gas has to be cooled immediately after leaving the tubular cracking furnace in order to prevent undesired side reactions which lead to a reduction in the yield of valuable products.
- This can be done directly by injecting liquid hydrocarbons or water into the hot cracked gas.
- direct cooling has the disadvantage that when the heat is recovered in the form of water vapor, the water vapor obtained has only a low pressure level.
- the process has a considerable disadvantage, namely the deposition of coke on the inner walls of both the cracked tubes in the tube furnace and the inlet hood and the cooling tubes in the downstream cracked gas cooler. Due to the insulating effect of the coke, the tube wall temperature of the canned tubes of the tubular cracking furnace increases and the pressure loss increases. In the downstream cracked gas cooler, the heat transfer is deteriorated by the coke deposit, so that the temperature of the cracked gas rises at the outlet of the cracked gas cooler. Once the coke deposits have reached a certain strength, the tube cracking furnace must be switched off together with the downstream cracking gas cooler and the coke removed.
- the canned tubes are generally freed of coke with a water vapor / air mixture or only with water vapor or with a mixture of water vapor and hydrogen (cf. DE-OS 19 48 635) at temperatures of 700 ° C to 1000 ° C .
- the cracked gas cooler is cleaned mechanically.
- This method is very complex and requires a longer one '' Shutdown time of the tube cracking furnace and therefore a corresponding loss of production in the ethylene plant.
- the tube cracking furnace is usually cooled.
- the cracked gas cooler is opened and the individual pipes of the cracked gas cooler, for example with more than 50 pipes, are used for mechanical cleaning, e.g. with a high-pressure water device, at a water pressure of usually 300 to 700 bar or in the case of very hard coke deposition by means of water / sand blasting from the coke freed.
- a major disadvantage of this method is that the material of the furnace is subjected to excessive stress as a result of the frequent cooling and subsequent heating, and damage often occurs as a result.
- the method described above is modified in such a way that one first cools the tube cracking furnace at 200 0 C to 400 ° C, then separating the gas cooler of the tube cracking furnace and performs the mechanical cleaning of completely cooled cleavage gas cooler, while the cracking tubes the cracked gas cooler with a water vapor / air mixture. But even here, only a small amount of time is saved, especially since the change in temperature and the stress on the canned tubes of the tubular cracking furnace can cause coke to separate from the inside of the canned tubes and thus create additional problems.
- the coke in the cracked gas cooler is only removed to a small extent due to the lower temperatures that arise in the one-line decoking in the cracked gas cooler.
- the disadvantage that the temperature at which the cracking gas emerges from the cracking gas cooler does not drop to the value of a mechanically cleaned cooler, but is only slightly lower than before the shutdown, so that a correspondingly smaller amount of high pressure steam is generated in the cracked gas cooler.
- mechanical cleaning of the cracked gas cooler with all the disadvantages described is necessary.
- the invention was therefore based on the object of a method for the thermal decoking of cracked gas coolers to make available, which does not have the disadvantages of the known methods.
- the cracked gas coolers can be decoked thermally without the need for additional mechanical cleaning of the cracked gas cooler and the associated cooling of the upstream tube cracking furnaces.
- the known methods for example in the one-line decoking described above, only annual runtimes of the tube cracking furnaces of 85 to 95% are achieved, annual runtimes of more than 97% and thus correspondingly are reduced by reducing the downtimes get higher ethylene production.
- fewer replacement tube cracking furnaces are required in the ethylene plant due to the increased operating time, which reduces the investment costs for the ethylene plant.
- cracked gas coolers are thermally decoked, which are used for indirect cooling by means of water of ethylene-containing cracked gases, the cracked gases being obtained by thermal cracking of hydrocarbons in the presence of steam in an indirectly heated tubular cracking furnace at gas outlet temperatures above 750 ° C.
- Suitable starting hydrocarbons for thermal cracking are ethane, propane, butane, LPG, gasoline fractions such as light petrol, e.g. light petrol with a boiling range of approx. 30 to 150 ° C, gasoline (full-range naphtha), e.g. gasoline with a boiling range of approx. 30 up to 180 ° C, heavy gasoline, e.g. heavy gasoline with a boiling range of approx.
- the method is preferably used for cracked gas coolers for cooling cracked gases obtained from gasoline fractions, kerosene and / or gas oils.
- the Austrittstem p eraturen of the cracking gas from the tubular cracking furnace amount to more than 750 ° C, preferably 780-900 ° C, in particular 800 to 900 ° C.
- the residence times in the tube cracking furnaces are generally 0.05 to 1 sec., Preferably 0.1 to 0.6 sec., In particular 0.1 to 0.5 sec.
- the thermal loads on the canned tubes in the tubular cracking furnaces are expediently 40,000 to 80,000 kcal / m 2 . h, v o rz UGS as 50,000 to 70,000 kcal / m 2 .h.
- the weight ratio of water vapor to the hydrocarbon used is L.
- thermal splitting generally 0.1: 1, preferably 0.2: 0.8, in particular 0.3: 0.7.
- heated air is passed through the cracked gas cooler to be decoked without the addition of water vapor. It is also possible to use heated mixtures of air and oxygen instead of heated air to accelerate decoking.
- the volume ratio of air to oxygen is generally 100: 1 to 1: 100, preferably 100: 1 to 1:50, in particular 100: 1 to 1:10 however, because of the easy availability, use heated air alone without additional oxygen for decoking.
- the cracked gas cooler inlet temperature for the heated air or the air / oxygen mixture is generally 600 to 1100 ° C, preferably 700 to 1050 ° C, in particular 800 to 1000 ° C.
- Decoking can be carried out while maintaining slightly reduced pressure in the cracked gas cooler, e.g. in the range of 0.5 to 1 bar.
- atmospheric pressure or increased pressure are used in the cracked gas cooler.
- the pressures are expediently 1 to 50 bar, preferably 1 to 20 bar, in particular 1 to 10 bar.
- elevated pressures of 2 to 50 bar, preferably 5 to 40 bar.
- the thermal decoking of the cracked gas cooler is expedient in the cracked gas cooler on the boiling side Water maintain a vapor pressure of 80 to 160 bar, preferably 90 to 150 bar, in particular 100 to 130 bar.
- the ratio of the amount of heated air or the heated air / oxygen mixture passed through per hour during the thermal decoking to the amount of hydrocarbon passed through per hour during the thermal cracking is 0.05 to 5, preferably 0.1 to 3 , in particular 0.1 to 2.
- the cracked gas cooler is decoked to such an extent that the exit temperature of the cracked gas from the cracked gas cooler corresponds to the initial value of the exit temperature of the cracked gas cooler from the cracked gas cooler at the start of the first start-up of the cracked gas cooler or after mechanical cleaning of the cracked gas cooler.
- the cracked gas cooler is completely freed of the coke after about 20 to 30 hours and then has the above-mentioned initial value of the starting temperature of the cracked gas after restarting.
- the course and the end of the decoking process can be followed in a simple manner by determining the carbon dioxide concentration in the gas mixture introduced into the cracked gas cooler and the gas mixture emerging from the cracked gas cooler.
- the air or the air / oxygen mixture can be heated in a separate oven, bypassing the tube cracking furnace or tubes belonging to the cracked gas cooler, to the cracked gas cooler inlet temperatures and passed through the cracked gas cooler.
- the air or the air / oxygen mixture in the associated tubular cracking furnaces is preferably heated to the inlet temperature for the cracked gas cooler and passed through the downstream cracked gas cooler.
- the cracked tubes of the upstream tube cracking furnace are first decoked. This is expediently carried out in such a way that, after the addition of the hydrocarbon to be split has been prevented, a water vapor / air mixture is passed through the indirectly heated cracking tubes of the tube cracking furnace and at the same time through the downstream cracking gas cooler, and after the decoking of the cracking tubes of the tube cracking furnace has ended, the water vapor supply is prevented and only air or the air / oxygen mixture are passed through the indirectly heated canned tubes of the tubular cracking furnace and the downstream cracked gas cooler.
- outlet temperatures for the gas mixture leaving the tube cracking furnace are generally used, which are between 600 and 11000C, preferably between 700 and 1050 ° C, in particular between 700 and 900 ° C .
- the water vapor / air mixture used expediently has a weight ratio of water vapor to air of 100: 1 to 2: 8, preferably 9: 1 to 3: 7, expediently using a water vapor / air mixture with a very low air content , for example less than 10% by weight of air, or water vapor alone begins and then rises 'Mixing sufficient amounts of air, for example up to an air content of 70% by weight in the water vapor / air mixture.
- a mixture of 2.2 t / h of a gasoline fraction (naphtha) with a boiling range of 40 to 180 ° C and 1.05 t / h of water vapor is passed through in a tube cracking furnace, which contains four cracking tubes, and at a furnace exit temperature of 850 ° C split.
- the cracked gas from 2 cracked tubes is cooled in a downstream cracked gas cooler.
- the cooler outlet temperature is 350 ° C.
- this cracked gas cooler outlet temperature finally rises to 450 ° C, the highest outlet temperature permitted for the cracked gas cooler.
- the hydrocarbon flow through the tube cracking furnace is interrupted and the cracked tubes and the cracked gas cooler are decoked in a conventional manner by passing a water vapor / air mixture through the cracked tubes and the downstream cracked gas cooler.
- 1.0 t / h of water vapor and 0.08 t / h of air are initially passed through each can.
- the air throughput is slowly increased and the water vapor throughput is reduced until finally a water vapor / air mixture with 70 vol.% Air is passed through each can. This state is maintained for a further 6 hours, so that the entire decoking process takes 16 hours.
- the tubular cracking furnace is operated as described in the first paragraph of the comparative example, initially to produce the cracked gas with the addition of naphtha and water vapor and, after reaching the maximum permissible cracked gas cooler outlet temperature of 450 ° C., is subjected to the decoking of 16 hours described in the first paragraph of the comparative example.
- the water vapor throughput is then completely prevented and only air in an amount of 1.3 t / h per can is passed through. This corresponds to a weight ratio of 0.59 of the amount of air passed per hour per can to the amount of hydrocarbon passed per hour during the thermal cracking.
- a furnace exit temperature of 850 0 C is maintained.
- a cracked gas cooler outlet temperature of 335 ° C is reached.
- High pressure steam of 125 bar continues to be generated during these 30 hours.
- the tube cracking furnace is again passed through by passing 2.2 t / h of naphtha and 1.05 t / h of steam each Canned tube put into operation.
- 2.2 t / h of gas oil and 1.7 t / h of water vapor are split in a tube cracking furnace at a furnace exit temperature of 830 ° C.
- the cracked gas cooler outlet temperature in the clean state is 550 ° C with a steam pressure on the water side of 125 bar.
- the cracked gas cooler outlet temperature rises to 650 ° C, the highest outlet temperature permitted for the cracked gas cooler.
- the hydrocarbon stream is interrupted and, as described in Example 1 and in the comparative example, first a mixture of water vapor and air with a slowly increasing air content (until a water vapor / air mixture with 70% by volume of air is reached) through the can and the downstream gas cooler passed.
- the canned tubes of the tubular cracking furnace are completely cleaned, while the cracked gas cooler has only been cleaned slightly.
- air alone is first heated without passing water vapor while passing through the cracking tubes of the tubular cracking furnace and then passed through the cracking gas cooler.
- a complete removal of coke from the cracked gas cooler is achieved after only 15 to 20 hours of passage of air, so that when the tube cracking furnace is put back into operation with the addition of gas oil and steam, the temperature of the cracked gas leaving the cracked gas cooler is again 550 ° C. in accordance with a mechanically cleaned one Cooler.
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Thermal Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Hydrogen, Water And Hydrids (AREA)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AT81101665T ATE5891T1 (de) | 1980-03-15 | 1981-03-07 | Verfahren zur thermischen entkokung von spaltgaskuehlern. |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE3010000 | 1980-03-15 | ||
DE19803010000 DE3010000A1 (de) | 1980-03-15 | 1980-03-15 | Verfahren zur thermischen entkokung von spaltgaskuehlern |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0036151A1 true EP0036151A1 (fr) | 1981-09-23 |
EP0036151B1 EP0036151B1 (fr) | 1984-01-18 |
EP0036151B2 EP0036151B2 (fr) | 1987-05-13 |
Family
ID=6097306
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP81101665A Expired EP0036151B2 (fr) | 1980-03-15 | 1981-03-07 | Procédé de décokage de refroidisseurs de gaz craqués |
Country Status (7)
Country | Link |
---|---|
US (1) | US4420343A (fr) |
EP (1) | EP0036151B2 (fr) |
JP (1) | JPS56142217A (fr) |
AT (1) | ATE5891T1 (fr) |
AU (1) | AU540068B2 (fr) |
CA (1) | CA1164385A (fr) |
DE (2) | DE3010000A1 (fr) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0497155A1 (fr) * | 1991-01-31 | 1992-08-05 | Linde Aktiengesellschaft | Procédé de décokéfaction de fours de pyrolyse |
EP0591856A1 (fr) * | 1992-10-05 | 1994-04-13 | Stone & Webster Engineering Corporation | Décokage à air pulsé |
FR2711374A1 (fr) * | 1993-10-20 | 1995-04-28 | Schmidt Sche Heissdampf | Procédé de décokage thermique d'un four de craquage et du refroidisseur de gaz de craquage en aval. |
FR2728578A1 (fr) * | 1994-12-26 | 1996-06-28 | Inst Francais Du Petrole | Procede de vapocraquage flexible et installation de vapocraquage correspondante |
FR2750140A1 (fr) * | 1996-06-25 | 1997-12-26 | Inst Francais Du Petrole | Installation de vapocraquage avec moyens de protection contre l'erosion |
EP2048217A2 (fr) | 2007-10-12 | 2009-04-15 | Linde Aktiengesellschaft | Procédé de décocage de fours de craquage |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6113774A (en) * | 1998-05-22 | 2000-09-05 | Phillips Petroleum Company | Antifoulant control process |
FR2837273B1 (fr) * | 2002-03-15 | 2004-10-22 | Inst Francais Du Petrole | Procede d'elimination au moins partielle de depots carbones dans un echangeur de chaleur |
US7465388B2 (en) * | 2005-07-08 | 2008-12-16 | Exxonmobil Chemical Patents Inc. | Method for processing hydrocarbon pyrolysis effluent |
US7763162B2 (en) * | 2005-07-08 | 2010-07-27 | Exxonmobil Chemical Patents Inc. | Method for processing hydrocarbon pyrolysis effluent |
US8524070B2 (en) * | 2005-07-08 | 2013-09-03 | Exxonmobil Chemical Patents Inc. | Method for processing hydrocarbon pyrolysis effluent |
US7749372B2 (en) * | 2005-07-08 | 2010-07-06 | Exxonmobil Chemical Patents Inc. | Method for processing hydrocarbon pyrolysis effluent |
US7780843B2 (en) * | 2005-07-08 | 2010-08-24 | ExxonMobil Chemical Company Patents Inc. | Method for processing hydrocarbon pyrolysis effluent |
CN100425940C (zh) * | 2005-10-21 | 2008-10-15 | 中国石油化工股份有限公司 | 一种大型管壳类换热设备管束的高温裂解除垢设备及除垢方法 |
FR3011556B1 (fr) * | 2013-10-09 | 2015-12-25 | Commissariat Energie Atomique | Procede de purification d'un gaz de synthese brut issu d'une pyrolyse et/ou gazeification d'une charge de matiere carbonee par destruction de goudrons contenus dans le gaz |
CN104327904A (zh) * | 2014-10-30 | 2015-02-04 | 北京晟辉兴业科技有限公司 | 一种液态锅炉结焦抑制剂 |
WO2024089443A1 (fr) * | 2022-10-25 | 2024-05-02 | Dow Global Technologies Llc | Procédé de décokage d'un four de craquage |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2289350A (en) * | 1937-12-29 | 1942-07-14 | Texas Co | Method of reconditioning furnace tubes |
US2671741A (en) * | 1950-02-23 | 1954-03-09 | Texas Co | Decoking and cleaning tubular heaters |
FR1432867A (fr) * | 1964-03-07 | 1966-03-25 | Basf Ag | Procédé de préparation de carbures éthyléniques, en particulier d'éthylène, par scission thermique d'hydrocarbures |
FR1532127A (fr) * | 1966-07-25 | 1968-07-05 | Idemitsu Petrochemical Co | Procédé perfectionné pour enlever les dépôts de carbone des appareils de craquage thermique |
DE1926495A1 (de) * | 1968-05-25 | 1970-02-05 | Mitsubishi Heavy Ind Ltd | Waermetauscher |
DE1948635A1 (de) * | 1968-10-16 | 1970-07-16 | Exxon Research Engineering Co | Entkokungsverfahren beim thermischen Kracken von Kohlenwasserstoffen |
EP0021167A1 (fr) * | 1979-06-08 | 1981-01-07 | Linde Aktiengesellschaft | Procédé et dispositif pour le décokage thermique d'un réacteur de craquage thermique d'hydrocarbures, le reacteur comportant une zone de craquage et un refroidisseur pour le gaz de craquage |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2057441A (en) * | 1935-05-15 | 1936-10-13 | Texas Co | Method of burning coke from heater tubes |
US2289351A (en) * | 1939-04-06 | 1942-07-14 | Texas Co | Method of cleaning heater tubes |
US2577254A (en) * | 1947-01-20 | 1951-12-04 | Phillips Petroleum Co | Removing carbon and carbonaceous deposits from heat exchanger equipment |
JPS503268B1 (fr) * | 1966-07-25 | 1975-02-01 | ||
US3507929A (en) * | 1966-11-30 | 1970-04-21 | John Happel | Decoking process for a pyrolysis reactor |
GB1255886A (en) * | 1969-04-23 | 1971-12-01 | Mitsui Shipbuilding Eng | Process and apparatus for preparing lower olefins |
-
1980
- 1980-03-15 DE DE19803010000 patent/DE3010000A1/de not_active Withdrawn
-
1981
- 1981-02-23 CA CA000371505A patent/CA1164385A/fr not_active Expired
- 1981-02-25 US US06/237,963 patent/US4420343A/en not_active Expired - Lifetime
- 1981-03-07 EP EP81101665A patent/EP0036151B2/fr not_active Expired
- 1981-03-07 DE DE8181101665T patent/DE3161916D1/de not_active Expired
- 1981-03-07 AT AT81101665T patent/ATE5891T1/de active
- 1981-03-13 AU AU68353/81A patent/AU540068B2/en not_active Expired
- 1981-03-13 JP JP3547481A patent/JPS56142217A/ja active Granted
Patent Citations (9)
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US2289350A (en) * | 1937-12-29 | 1942-07-14 | Texas Co | Method of reconditioning furnace tubes |
US2671741A (en) * | 1950-02-23 | 1954-03-09 | Texas Co | Decoking and cleaning tubular heaters |
FR1432867A (fr) * | 1964-03-07 | 1966-03-25 | Basf Ag | Procédé de préparation de carbures éthyléniques, en particulier d'éthylène, par scission thermique d'hydrocarbures |
FR1532127A (fr) * | 1966-07-25 | 1968-07-05 | Idemitsu Petrochemical Co | Procédé perfectionné pour enlever les dépôts de carbone des appareils de craquage thermique |
DE1926495A1 (de) * | 1968-05-25 | 1970-02-05 | Mitsubishi Heavy Ind Ltd | Waermetauscher |
US3570458A (en) * | 1968-05-25 | 1971-03-16 | Mitsubishi Heavy Ind Ltd | Heat exchanger construction |
DE1948635A1 (de) * | 1968-10-16 | 1970-07-16 | Exxon Research Engineering Co | Entkokungsverfahren beim thermischen Kracken von Kohlenwasserstoffen |
US3557241A (en) * | 1968-10-16 | 1971-01-19 | Exxon Research Engineering Co | Decoking of onstream thermal cracking tubes with h20 and h2 |
EP0021167A1 (fr) * | 1979-06-08 | 1981-01-07 | Linde Aktiengesellschaft | Procédé et dispositif pour le décokage thermique d'un réacteur de craquage thermique d'hydrocarbures, le reacteur comportant une zone de craquage et un refroidisseur pour le gaz de craquage |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0497155A1 (fr) * | 1991-01-31 | 1992-08-05 | Linde Aktiengesellschaft | Procédé de décokéfaction de fours de pyrolyse |
EP0591856A1 (fr) * | 1992-10-05 | 1994-04-13 | Stone & Webster Engineering Corporation | Décokage à air pulsé |
FR2711374A1 (fr) * | 1993-10-20 | 1995-04-28 | Schmidt Sche Heissdampf | Procédé de décokage thermique d'un four de craquage et du refroidisseur de gaz de craquage en aval. |
FR2728578A1 (fr) * | 1994-12-26 | 1996-06-28 | Inst Francais Du Petrole | Procede de vapocraquage flexible et installation de vapocraquage correspondante |
WO1996020255A1 (fr) * | 1994-12-26 | 1996-07-04 | Institut Francais Du Petrole | Procede de vaprocraquage flexible et installation de vapocraquage correspondante |
FR2750140A1 (fr) * | 1996-06-25 | 1997-12-26 | Inst Francais Du Petrole | Installation de vapocraquage avec moyens de protection contre l'erosion |
WO1997049782A1 (fr) * | 1996-06-25 | 1997-12-31 | Institut Francais Du Petrole | Installation de vapocraquage avec moyens de protection contre l'erosion |
US6464949B1 (en) | 1996-06-25 | 2002-10-15 | Institut Francais Du Petrole | Steam cracking installation with means for protection against erosion |
EP2048217A2 (fr) | 2007-10-12 | 2009-04-15 | Linde Aktiengesellschaft | Procédé de décocage de fours de craquage |
EP2048217A3 (fr) * | 2007-10-12 | 2012-06-06 | Linde AG | Procédé de décocage de fours de craquage |
Also Published As
Publication number | Publication date |
---|---|
DE3010000A1 (de) | 1981-09-24 |
AU6835381A (en) | 1981-09-24 |
US4420343A (en) | 1983-12-13 |
JPS56142217A (en) | 1981-11-06 |
DE3161916D1 (en) | 1984-02-23 |
EP0036151B1 (fr) | 1984-01-18 |
CA1164385A (fr) | 1984-03-27 |
JPH0113515B2 (fr) | 1989-03-07 |
ATE5891T1 (de) | 1984-02-15 |
AU540068B2 (en) | 1984-11-01 |
EP0036151B2 (fr) | 1987-05-13 |
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