US3718709A - Process for producing ethylene - Google Patents
Process for producing ethylene Download PDFInfo
- Publication number
- US3718709A US3718709A US00060149A US3718709DA US3718709A US 3718709 A US3718709 A US 3718709A US 00060149 A US00060149 A US 00060149A US 3718709D A US3718709D A US 3718709DA US 3718709 A US3718709 A US 3718709A
- Authority
- US
- United States
- Prior art keywords
- weight
- steam
- pyrolysis
- hydrocarbon
- hydrocarbons
- 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.)
- Expired - Lifetime
Links
Classifications
-
- 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
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
Definitions
- R ponents a further amount of superheated teal is added to obtain a feed at 450-550 C for a tubular [51] Int. Cl ..C07c 3/00 pyrolysis reactor operating at 700 4 00 0
- the total steam content in the feed is 0.5 to 5.0 parts by weight [58] Field of Search ..260/683; 208/130 steam per part by weight of the hydrocarbon.
- the present invention concerns the production of ethylene by pyrolysis of fuel oils.
- this invention concerns the production of gaseous mixtures having an ethylene content exceeding 40 percent by weight, by pyrolysis, in the presence of steam, of heavy hydrocarbon mixtures having an initial boiling point in excess of 300C, particularly heavy fuel oils.
- a number of industrial methods are known for the pyrolysis of normally gaseous hydrocarbons such as the natural gases, ethane, propane, butane or relatively light hydrocarbon liquids, for example, the mixture of hydrocarbons found in commerce and known as Naphtha.
- Certain pyrolysis processes utilize hydrocarbon mixtures (e.g., crude petroleum) containing low boiling liquid fractions.
- the low boiling liquid fractions are first separated from their mother-mixture (for example by means of steam) and the pyrolysis is carried out on only these separated fractions.
- the hydrocarbons are subjected to elevated temperatures for a very short period, the products of the pyrolysis then being cooled rapidly and finally fractionated.
- gaseous mixtures having an ethylene content exceeding 40 percent by weight can be obtained by high-temperature pyrolysis, in the presence of steam, of hydrocarbon mixtures having an initial boiling point exceeding 300C, in particular by pyrolysis of heavy fuel oils.
- the process of the present invention is advantageously carried out by use of a cyclically operated tube-furnace in which the periods of pyrolysis are alternated with periods of regeneration to eliminate the deposits of coke within the tubes, although the quantity of deposited coke does not become excessive (less than 1 percent in proportion to the oil introduced) in the tube furnace during operation of the present process.
- This regeneration is conventional and is preferably effected at temperatures of 750 to 900C, by passing a mixture of air and steam through the pyrolysis tube furnace.
- the hydrocarbon is first preheated and then mixed with primary steam in a proportion of 0.1 to 0.5 parts by weight to each part by weight of hydrocarbon.
- the secondary steam in a proportion such that the weight ratio of steam/hydrocarbon at the inlet to the pyrolysis furnace is between 0.5 to 5.0 and preferably between 1.5 and 3.0
- the temperature of the mixture may vary between 450 and 550C.
- the hydrocarbons are pyrolysed, the temperature of the interior of the tubes preferably being maintained between 700 and 800C and the residence time of the mixture in the reactor proper being maintained between 1 and 3 seconds, preferably 1.5 and 2 seconds.
- the hydrocarbons in the pyrolysis furnace are converted to normally gaseous products in an amount up to 50 wt. percent of the hydrocarbon feed.
- the composition of the feed steam: hydrocarbon
- the pyrolysis conditions prevent coke formation in furnace tubes and contribute towards formation of ethylene-rich pyrolysis gases from the specific hydrocarbon stock employed.
- the pyrolysis product leaving the pyrolysis reactor is quenched to about 300 to 400C, preferably by admixture of the product with water to make use of the heat of vaporization of the latter.
- the products are thus separated into liquids and gases which are then fractionated.
- a pryolysis gas is obtained in which the content of ethylene exceeds 40 percent by weight, thus allowing subsequent separation to be effected in a very economical manner.
- the present process has the advantage of utilizing inexpensive starting materials, such as heavy fuel oils or other heavy petroleum fractions.
- Flow pointt36C Lower calorific value 9,800 calories/kg Boiling point: 380C
- the oil is preheated and mixed with about 23 kg/h superheated steam at a temperature of 500C.
- the mixture, at a temperature of 360C and pressure of 1.1 atm. abs. is passed through a gas-liquid separator.
- the gaseous products obtained are admixed with about 93 kg/h of superheated steam at a temperature of 780C.
- the new mixture containing about 27 by weight hydrocarbons, is introduced at a temperature of 530C and under 1.1 atm. abs. into a pyrolysis reactor formed by a tube furnace heated from the outside.
- the pyrolysis conditions correspond to a residence time of the mixture of 1.7 seconds, the products reaching the furnace outlet at a temperature of about 770C.
- the products leaving the reactor are quenched to about 400C in a mixing tower fed with about 43 kg/h water which is instantly vaporized.
- the heavier hydrocarbons are separated in a separating tower at a temperature of about 110 C, while the lighter products constituting the pyrolysis gas, the water and the hydrocarbons boiling at about the boiling point of petrol are successively cooled in a heat exchanger.
- the pyrolysis product has the following composition determined by gas chromatography methane 24.9% by weight ethylene 46.3% by weight ethane 4.5% by weight C hydrocarbons 8.6% by weight C. hydrocarbons 2.9% by weight benzene 3.8% by weight water 1.8% by weight CO 2.8% by weight CO, 2.2% by weight hydrogen 2.2% by weight
- pyrolysis periods of 10 to 12 hours can be alternated with regeneration periods of to minutes. This regeneration operation is effected at temperatures exceeding preferably by 100 C the pyrolysis temperature, that is to say between 750 and 950 C by passing air and steam at a rate of 20 to 50 m /h.
- a process for the production of a gaseous mixture containing above 40 wt. percent ethylene comprising:
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Hydrocarbons having a boiling point above 300* C (fuel oils) are vaporized by means of direct superheated steam; after separation of any liquid components a further amount of superheated steam is added to obtain a feed at 450* -550* C for a tubular pyrolysis reactor operating at 700*-800*C. The total steam content in the feed is 0.5 to 5.0 parts by weight steam per part by weight of the hydrocarbon.
Description
United States Patent 1191 Simonetta [4 1 Feb. 27, 1973 PROCESS FOR PRODUCING [56] References Cited ETHYLENE UNITED STATES PATENTS i {75] Inventor Mass Italy 2,363,903 11/1944 Smith ..260/668 [73] Assignee: Societa Italiana Resine S.l.R. S,p.A., 2,366,521 1/1945 Guicheh 6/ Milan Italy 3,103,485 9/1963 208/130 3,579,601 5/1971 260/683 [22] Filed: July 31, 1970 3,487,121 12/1969 260/683 3,597,494 8/1971 Bigache et al...... ...208/130 1 1 pp ,149 3,579,438 5/1971 Cruse ..208/l30 Related Application Data Primary Examiner-Delbert E. Gantz [63] Continuation-impart of Ser. No. 705,578, Feb. 12, Amstam Examiner j' Nelson 1958 abandone Att0rneySughrue, Rothwell, M1on, Zmn & Macpeak [30] Foreign Application Priority Data [57] ABSTRACT Hydrocarbons having a boiling point above 300 C Feb.23, 1967 Italy ..l2962 A/67 (fuel oils) are vaporized by means of direct supw heated steam; after separation of any liquid com- US. Cl. 6 R, R ponents a further amount of superheated teal is added to obtain a feed at 450-550 C for a tubular [51] Int. Cl ..C07c 3/00 pyrolysis reactor operating at 700 4 00 0 The total steam content in the feed is 0.5 to 5.0 parts by weight [58] Field of Search ..260/683; 208/130 steam per part by weight of the hydrocarbon.
7 Claims, No Drawings PROCESS FOR PRODUCING ETIIYLENE CROSS REFERENCE This application is a continuation-in-part of applicants copending application Ser. No. 704,578, filed Feb. 12, 1958, now abandoned.
BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention concerns the production of ethylene by pyrolysis of fuel oils.
More particularly, this invention concerns the production of gaseous mixtures having an ethylene content exceeding 40 percent by weight, by pyrolysis, in the presence of steam, of heavy hydrocarbon mixtures having an initial boiling point in excess of 300C, particularly heavy fuel oils.
2. Description of the Prior Art In latter years, ethylene has attained very great importance in a variety of fields, such as the preparation of plastic materials or in modern processes for obtaining products formerly prepared from acetylene. For these reasons, the demand for this compound has been greatly increased and production techniques have been correspondingly improved.
At the present time, the pyrolysis of hydrocarbons is the process which is by far the most used for the production of ethylene.
A number of industrial methods are known for the pyrolysis of normally gaseous hydrocarbons such as the natural gases, ethane, propane, butane or relatively light hydrocarbon liquids, for example, the mixture of hydrocarbons found in commerce and known as Naphtha.
Certain pyrolysis processes utilize hydrocarbon mixtures (e.g., crude petroleum) containing low boiling liquid fractions. In said processes, the low boiling liquid fractions are first separated from their mother-mixture (for example by means of steam) and the pyrolysis is carried out on only these separated fractions. In pyrolysis processes carried out in the presence of steam, the hydrocarbons are subjected to elevated temperatures for a very short period, the products of the pyrolysis then being cooled rapidly and finally fractionated.
These procedures are inconvenient in that they utilize primary feed materials which are relatively expensive in the production of pyrolysis products having a concentration of ethylene not greater than about 30 percent by weight.
It has now been discovered that gaseous mixtures having an ethylene content exceeding 40 percent by weight can be obtained by high-temperature pyrolysis, in the presence of steam, of hydrocarbon mixtures having an initial boiling point exceeding 300C, in particular by pyrolysis of heavy fuel oils.
SUMMARY OF THE INVENTION The process of this invention comprises:
a. vaporizing an amount up to 50 wt. percent of a hydrocarbon mixture having an initial boiling point above 300C by admixture with 0.1 to 0.5 partsby weight of superheated steam (primary steam) per part by weight of the hydrocarbon mixture charge;
b. separating liquid components from gaseous components at a temperature of 300 to 450C; point c. admixing the gaseous components with a further amount of superheated steam (secondary steam) thereby to obtain, as the feed for a pyrolysis reaction, a mixture of steam and hydrocarbons at a temperature of 450 to 550C, which mixture contains 0.5 to 5.0 parts by weight of steam per each part by weight of hydrocarbons;
d. pyrolysing said feed, for example, in a tubular reaction zone at a temperature of 700 to 800C over a period of from 1 to 3 seconds, thus producing from said feed an amount of normally gaseous hydrocarbons up to 50 wt. percent with respect to the hydrocarbons contained in the feed;
e. recovering said normally gaseous hydrocarbons from the pyrolysis product obtained.
DETAILED DESCRIPTION OF THE INVENTION As in previous processes of this type, the process of the present invention is advantageously carried out by use of a cyclically operated tube-furnace in which the periods of pyrolysis are alternated with periods of regeneration to eliminate the deposits of coke within the tubes, although the quantity of deposited coke does not become excessive (less than 1 percent in proportion to the oil introduced) in the tube furnace during operation of the present process. This regeneration is conventional and is preferably effected at temperatures of 750 to 900C, by passing a mixture of air and steam through the pyrolysis tube furnace.
In the process of the present invention, the hydrocarbon is first preheated and then mixed with primary steam in a proportion of 0.1 to 0.5 parts by weight to each part by weight of hydrocarbon.
As a result, a mixture comprising a gaseous phase and a liquid phase at 300-450C is obtained, from which the liquid phase is subsequently separated in a gas/liquid separator maintained within this temperature range. By operating under these conditions, an amount of up to 50 wt. percent of hydrocarbon components is vaporized. It should be pointed out that, considering the nature of the hydrocarbon charge employed, a vaporization of an amount exceeding 50 percent hydrocarbons would give rise to undesirable deposits in the gas/liquid separator comprising carbonaceous and/or pitchy residues. Moreover, the hydrocarbons which would then be present in the feed to the pyrolysis furnace would contain undesirably high amounts of fractions capable of immediately coking in the furnace (with consequent clogging of the furnace tubes). Thus, it is important to partially vaporize the hydrocarbon charge using only a relatively small amount of steam and to dilute the vaporized fraction with a further amount of steam only subsequently to the initial vaporization and separation steps.
To the gaseous mixture thus obtained is added the secondary steam in a proportion such that the weight ratio of steam/hydrocarbon at the inlet to the pyrolysis furnace is between 0.5 to 5.0 and preferably between 1.5 and 3.0 The temperature of the mixture may vary between 450 and 550C.
In the pyrolysis furnace, formed of tubes heated from the outside, the hydrocarbons are pyrolysed, the temperature of the interior of the tubes preferably being maintained between 700 and 800C and the residence time of the mixture in the reactor proper being maintained between 1 and 3 seconds, preferably 1.5 and 2 seconds.
By operating under these conditions, the hydrocarbons in the pyrolysis furnace are converted to normally gaseous products in an amount up to 50 wt. percent of the hydrocarbon feed. The composition of the feed (steam: hydrocarbon) is to be maintained within the limits stated hereinbefore, in order to avoid deposits of coke in the furnace tubes. Moreover, the pyrolysis conditions (relatively high temperatures and short residence times) prevent coke formation in furnace tubes and contribute towards formation of ethylene-rich pyrolysis gases from the specific hydrocarbon stock employed.
The pyrolysis product leaving the pyrolysis reactor is quenched to about 300 to 400C, preferably by admixture of the product with water to make use of the heat of vaporization of the latter. The products are thus separated into liquids and gases which are then fractionated.
The values set forth above with regard to the amount of hydrocarbon stock to be vaporized by admixture with primary steam (50 wt. percent) and the amount of conversion of hydrocarbon pyrolysis feed into normally gaseous hydrocarbons (50 wt. percent) are to be considered as maximums for operation in accordance with the present invention. Any positive value less than these is operable in the process of the present invention, the minimum acceptable values being dictated by purely economical considerations.
Employing the process of the present invention, a pryolysis gas is obtained in which the content of ethylene exceeds 40 percent by weight, thus allowing subsequent separation to be effected in a very economical manner.
Finally, the present process has the advantage of utilizing inexpensive starting materials, such as heavy fuel oils or other heavy petroleum fractions.
The following example illustrates the present invention without limiting the scope thereof.
EXAMPLE A pilot plant is fed with 100 kg/h of a fuel oil having the following characteristics:
API: 20.4
Flow pointt36C Lower calorific value 9,800 calories/kg Boiling point: 380C The oil is preheated and mixed with about 23 kg/h superheated steam at a temperature of 500C. The mixture, at a temperature of 360C and pressure of 1.1 atm. abs. is passed through a gas-liquid separator.
The gaseous products obtained are admixed with about 93 kg/h of superheated steam at a temperature of 780C. The new mixture, containing about 27 by weight hydrocarbons, is introduced at a temperature of 530C and under 1.1 atm. abs. into a pyrolysis reactor formed by a tube furnace heated from the outside.
The pyrolysis conditions correspond to a residence time of the mixture of 1.7 seconds, the products reaching the furnace outlet at a temperature of about 770C. The products leaving the reactor are quenched to about 400C in a mixing tower fed with about 43 kg/h water which is instantly vaporized.
The heavier hydrocarbons are separated in a separating tower at a temperature of about 110 C, while the lighter products constituting the pyrolysis gas, the water and the hydrocarbons boiling at about the boiling point of petrol are successively cooled in a heat exchanger.
In this manner, normally gaseous products are recovered which can be separated by normal techniques at a rate of 24 to 24.5 kg/h, calculated as dry products.
The pyrolysis product has the following composition determined by gas chromatography methane 24.9% by weight ethylene 46.3% by weight ethane 4.5% by weight C hydrocarbons 8.6% by weight C. hydrocarbons 2.9% by weight benzene 3.8% by weight water 1.8% by weight CO 2.8% by weight CO, 2.2% by weight hydrogen 2.2% by weight In a series of tests with the pilot plant described, pyrolysis periods of 10 to 12 hours can be alternated with regeneration periods of to minutes. This regeneration operation is effected at temperatures exceeding preferably by 100 C the pyrolysis temperature, that is to say between 750 and 950 C by passing air and steam at a rate of 20 to 50 m /h.
What is claimed is:
l. A process for the production of a gaseous mixture containing above 40 wt. percent ethylene comprising:
a. vaporizing up to 50 wt. of a heavy fuel oil hydrocarbon mixture having an initial boiling point above 300C by admixing said mixture with 0.1 to 0.5 parts by weight of superheated steam per part by weight of hydrocarbon separating liquid components from gaseous components by passing said mixture through a gasliquid separator at a temperature of 300 to 45C c. admixing said gaseous components with a further amount of superheated steam to obtain a feed mixture of steam and hydrocarbons having a temperature of from 450 to 550C, the total proportion of steam present in said feed mixture being from 0.5 to 5.0 parts by weight per part by weight of hydrocarbon,
d. pyrolyzing said feed mixture at a temperature of 700 to 800C for from 1 to 3 seconds to produce normally gaseous hydrocarbons in an amount of up to 50 wt. percent of the weight of hydrocarbons subjected to pyrolysis, and
e. recovering said normally gaseous hydrocarbons from the pyrolysis product obtained.
2. The process of claim 1 wherein the hydrocarbon mixture is a heavy fuel oil.
3. The process according to claim 1 wherein the proportion of steam present in said feed mixture is from 1.5 to 3.0 parts by weight per part by weight of the hydrocarbon.
4. The process according to claim 1 wherein said feed mixture is pyrolyzed for from 1.5 to 2 seconds.
5. The process according to claim 1 wherein said normally gaseous hydrocarbons are quenched to about 300 to 400C.
6. The process according to claim 5 wherein said normally gaseous hydrocarbons are quenched with water.
7. The process according to claim 1 whereby deposits of coke are reduced. 5
Claims (6)
- 2. The process of claim 1 wherein the hydrocarbon mixture is a heavy fuel oil.
- 3. The process according to claim 1 wherein the proportion of steam present in said feed mixture is from 1.5 to 3.0 parts by weight per part by weight of the hydrocarbon.
- 4. The process according to claim 1 wherein said feed mixture is pyrolyzed for from 1.5 to 2 seconds.
- 5. The process according to claim 1 wherein said normally gaseous hydrocarbons are quenched to about 300* to 400*C.
- 6. The process according to claim 5 wherein said normally gaseous hydrocarbons are quenched with water.
- 7. The process according to claim 1 whereby deposits of coke are reduced.
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
IT1296267 | 1967-02-23 |
Publications (1)
Publication Number | Publication Date |
---|---|
US3718709A true US3718709A (en) | 1973-02-27 |
Family
ID=11143934
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US00060149A Expired - Lifetime US3718709A (en) | 1967-02-23 | 1970-07-31 | Process for producing ethylene |
Country Status (3)
Country | Link |
---|---|
US (1) | US3718709A (en) |
DE (1) | DE1668674A1 (en) |
NL (1) | NL6802193A (en) |
Cited By (31)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4479869A (en) * | 1983-12-14 | 1984-10-30 | The M. W. Kellogg Company | Flexible feed pyrolysis process |
US4527002A (en) * | 1983-02-18 | 1985-07-02 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking method for producing olefines from hydrocarbons |
US4527003A (en) * | 1983-03-03 | 1985-07-02 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking process for producing olefins from hydrocarbons |
US4655904A (en) * | 1983-06-17 | 1987-04-07 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking process for selectively producing olefins and aromatic hydrocarbons from hydrocarbons |
US4725349A (en) * | 1984-04-13 | 1988-02-16 | Mitsubishi Jukogyo Kabushiki Kaisha | Process for the selective production of petrochemical products |
US20040004027A1 (en) * | 2002-07-03 | 2004-01-08 | Spicer David B. | Process for cracking hydrocarbon feed with water substitution |
US20040004028A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Converting mist flow to annular flow in thermal cracking application |
US20040004022A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Process for steam cracking heavy hydrocarbon feedstocks |
US20050209495A1 (en) * | 2004-03-22 | 2005-09-22 | Mccoy James N | Process for steam cracking heavy hydrocarbon feedstocks |
US20050261535A1 (en) * | 2004-05-21 | 2005-11-24 | David Beattie | Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
US20050261530A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid |
US20050261538A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks |
US20050261531A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid |
US20050261533A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
US20050261532A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids |
US20050261537A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Steam cracking of hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
US20050261534A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace |
US20050261536A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking |
WO2005113718A2 (en) | 2004-05-21 | 2005-12-01 | Exxonmobil Chemical Patents Inc. | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
US20060014993A1 (en) * | 2004-07-14 | 2006-01-19 | Stell Richard C | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US20060014992A1 (en) * | 2004-07-14 | 2006-01-19 | Stell Richard C | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US20060014994A1 (en) * | 2004-07-16 | 2006-01-19 | Keusenkothen Paul F | Reduction of total sulfur in crude and condensate cracking |
US20060089519A1 (en) * | 2004-05-21 | 2006-04-27 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation |
US20060094918A1 (en) * | 2004-10-28 | 2006-05-04 | Mccoy James N | Steam cracking of hydrocarbon feedstocks containing salt and/or particulate matter |
US20060129012A1 (en) * | 2004-12-10 | 2006-06-15 | Frye James M | Vapor/liquid separation apparatus |
US20070004952A1 (en) * | 2005-06-30 | 2007-01-04 | Mccoy James N | Steam cracking of partially desalted hydrocarbon feedstocks |
US20090050530A1 (en) * | 2007-08-21 | 2009-02-26 | Spicer David B | Process and Apparatus for Steam Cracking Hydrocarbon Feedstocks |
KR100945121B1 (en) * | 2002-07-03 | 2010-03-02 | 엑손모빌 케미칼 패턴츠 인코포레이티드 | Converting mist flow to annular flow in thermal cracking application |
US20100300936A1 (en) * | 2009-05-29 | 2010-12-02 | Stell Richard C | Method and Apparatus for Recycle of Knockout Drum Bottoms |
US8118996B2 (en) | 2007-03-09 | 2012-02-21 | Exxonmobil Chemical Patents Inc. | Apparatus and process for cracking hydrocarbonaceous feed utilizing a pre-quenching oil containing crackable components |
KR20200123476A (en) * | 2018-03-13 | 2020-10-29 | 루머스 테크놀로지 엘엘씨 | In-situ caulking of heavy pitches and other feedstocks with high fouling tendency |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2363903A (en) * | 1941-01-02 | 1944-11-28 | Standard Oil Dev Co | Treating hydrocarbon fluids |
US2366521A (en) * | 1943-02-25 | 1945-01-02 | Standard Oil Dev Co | Method of removing coke deposits from high-temperature oil lines |
US3103485A (en) * | 1960-02-12 | 1963-09-10 | Temperature | |
US3487121A (en) * | 1966-06-13 | 1969-12-30 | Stone & Webster Eng Corp | Hydrocarbon process |
US3579601A (en) * | 1968-06-10 | 1971-05-18 | Exxon Research Engineering Co | Pyrolysis of hydrocarbons |
US3579438A (en) * | 1970-04-20 | 1971-05-18 | Monsanto Co | Thermal cracking |
US3597494A (en) * | 1968-09-04 | 1971-08-03 | Inst Francais Du Petrole | Steam-cracking of hydrocarbons |
-
1968
- 1968-02-15 NL NL6802193A patent/NL6802193A/xx unknown
- 1968-02-22 DE DE19681668674 patent/DE1668674A1/en active Pending
-
1970
- 1970-07-31 US US00060149A patent/US3718709A/en not_active Expired - Lifetime
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2363903A (en) * | 1941-01-02 | 1944-11-28 | Standard Oil Dev Co | Treating hydrocarbon fluids |
US2366521A (en) * | 1943-02-25 | 1945-01-02 | Standard Oil Dev Co | Method of removing coke deposits from high-temperature oil lines |
US3103485A (en) * | 1960-02-12 | 1963-09-10 | Temperature | |
US3487121A (en) * | 1966-06-13 | 1969-12-30 | Stone & Webster Eng Corp | Hydrocarbon process |
US3579601A (en) * | 1968-06-10 | 1971-05-18 | Exxon Research Engineering Co | Pyrolysis of hydrocarbons |
US3597494A (en) * | 1968-09-04 | 1971-08-03 | Inst Francais Du Petrole | Steam-cracking of hydrocarbons |
US3579438A (en) * | 1970-04-20 | 1971-05-18 | Monsanto Co | Thermal cracking |
Cited By (85)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4527002A (en) * | 1983-02-18 | 1985-07-02 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking method for producing olefines from hydrocarbons |
US4527003A (en) * | 1983-03-03 | 1985-07-02 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking process for producing olefins from hydrocarbons |
US4655904A (en) * | 1983-06-17 | 1987-04-07 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking process for selectively producing olefins and aromatic hydrocarbons from hydrocarbons |
US4479869A (en) * | 1983-12-14 | 1984-10-30 | The M. W. Kellogg Company | Flexible feed pyrolysis process |
US4725349A (en) * | 1984-04-13 | 1988-02-16 | Mitsubishi Jukogyo Kabushiki Kaisha | Process for the selective production of petrochemical products |
US20060249428A1 (en) * | 2002-07-03 | 2006-11-09 | Stell Richard C | Process for steam cracking heavy hydrocarbon feedstocks |
US20040004028A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Converting mist flow to annular flow in thermal cracking application |
US20040004022A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Process for steam cracking heavy hydrocarbon feedstocks |
US7578929B2 (en) | 2002-07-03 | 2009-08-25 | Exxonmoil Chemical Patents Inc. | Process for steam cracking heavy hydrocarbon feedstocks |
US7138047B2 (en) | 2002-07-03 | 2006-11-21 | Exxonmobil Chemical Patents Inc. | Process for steam cracking heavy hydrocarbon feedstocks |
US20040004027A1 (en) * | 2002-07-03 | 2004-01-08 | Spicer David B. | Process for cracking hydrocarbon feed with water substitution |
US7097758B2 (en) | 2002-07-03 | 2006-08-29 | Exxonmobil Chemical Patents Inc. | Converting mist flow to annular flow in thermal cracking application |
US7090765B2 (en) | 2002-07-03 | 2006-08-15 | Exxonmobil Chemical Patents Inc. | Process for cracking hydrocarbon feed with water substitution |
KR100945121B1 (en) * | 2002-07-03 | 2010-03-02 | 엑손모빌 케미칼 패턴츠 인코포레이티드 | Converting mist flow to annular flow in thermal cracking application |
US20050209495A1 (en) * | 2004-03-22 | 2005-09-22 | Mccoy James N | Process for steam cracking heavy hydrocarbon feedstocks |
WO2005095548A1 (en) | 2004-03-22 | 2005-10-13 | Exxonmobil Chemical Patents Inc. | Process for steam cracking heavy hydrocarbon feedstocks |
US7820035B2 (en) | 2004-03-22 | 2010-10-26 | Exxonmobilchemical Patents Inc. | Process for steam cracking heavy hydrocarbon feedstocks |
US20060213810A1 (en) * | 2004-05-21 | 2006-09-28 | Stell Richard C | Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking |
US20070049783A1 (en) * | 2004-05-21 | 2007-03-01 | Stell Richard C | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
WO2005113718A2 (en) | 2004-05-21 | 2005-12-01 | Exxonmobil Chemical Patents Inc. | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
WO2005113716A2 (en) | 2004-05-21 | 2005-12-01 | Exxonmobil Chemical Patents Inc. | Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace |
US20050261534A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace |
US7993435B2 (en) | 2004-05-21 | 2011-08-09 | Exxonmobil Chemical Patents Inc. | Process and apparatus for cracking hydrocarbon feedstock containing resid |
US20050261537A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Steam cracking of hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
WO2005113722A3 (en) * | 2004-05-21 | 2006-01-26 | Exxonmobil Chem Patents Inc | Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
US20060089519A1 (en) * | 2004-05-21 | 2006-04-27 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation |
US7767170B2 (en) | 2004-05-21 | 2010-08-03 | Exxonmobil Chemical Patents Inc. | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
US20050261532A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids |
US20050261533A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
US20050261531A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid |
US7470409B2 (en) | 2004-05-21 | 2008-12-30 | Exxonmobil Chemical Patents Inc. | Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks |
US20060226048A1 (en) * | 2004-05-21 | 2006-10-12 | Stell Richard C | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
US20050261538A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks |
US20050261530A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid |
US7670573B2 (en) | 2004-05-21 | 2010-03-02 | Exxonmobil Chemical Patents Inc. | Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids |
US20070006733A1 (en) * | 2004-05-21 | 2007-01-11 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid |
US20070009407A1 (en) * | 2004-05-21 | 2007-01-11 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid |
US20070031306A1 (en) * | 2004-05-21 | 2007-02-08 | Stell Richard C | Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks |
US20070031307A1 (en) * | 2004-05-21 | 2007-02-08 | Stell Richard C | Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids |
US20070029160A1 (en) * | 2004-05-21 | 2007-02-08 | Stell Richard C | Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks |
US20050261536A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking |
US7193123B2 (en) | 2004-05-21 | 2007-03-20 | Exxonmobil Chemical Patents Inc. | Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation |
US7220887B2 (en) | 2004-05-21 | 2007-05-22 | Exxonmobil Chemical Patents Inc. | Process and apparatus for cracking hydrocarbon feedstock containing resid |
US7235705B2 (en) | 2004-05-21 | 2007-06-26 | Exxonmobil Chemical Patents Inc. | Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks |
US20070160513A1 (en) * | 2004-05-21 | 2007-07-12 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation |
US7244871B2 (en) | 2004-05-21 | 2007-07-17 | Exxonmobil Chemical Patents, Inc. | Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids |
US7247765B2 (en) | 2004-05-21 | 2007-07-24 | Exxonmobil Chemical Patents Inc. | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
US20070215524A1 (en) * | 2004-05-21 | 2007-09-20 | Stell Richard C | Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid |
CN100587032C (en) | 2004-05-21 | 2010-02-03 | 埃克森美孚化学专利公司 | Steam cracking of light hydrocarbon raw material containing non-volatile components and/or coke precursors |
US7297833B2 (en) | 2004-05-21 | 2007-11-20 | Exxonmobil Chemical Patents Inc. | Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
US7312371B2 (en) | 2004-05-21 | 2007-12-25 | Exxonmobil Chemical Patents Inc. | Steam cracking of hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
US7311746B2 (en) | 2004-05-21 | 2007-12-25 | Exxonmobil Chemical Patents Inc. | Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid |
US7351872B2 (en) | 2004-05-21 | 2008-04-01 | Exxonmobil Chemical Patents Inc. | Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace |
US7588737B2 (en) | 2004-05-21 | 2009-09-15 | Exxonmobil Chemical Patents Inc. | Process and apparatus for cracking hydrocarbon feedstock containing resid |
US20050261535A1 (en) * | 2004-05-21 | 2005-11-24 | David Beattie | Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
US20080119679A1 (en) * | 2004-05-21 | 2008-05-22 | Stell Richard C | Process And Draft Control System For Use In Cracking A Heavy Hydrocarbon Feedstock In A Pyrolysis Furnace |
US7553460B2 (en) | 2004-05-21 | 2009-06-30 | Exxonmobil Chemical Patents Inc. | Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation |
US7544852B2 (en) | 2004-05-21 | 2009-06-09 | Exxonmobil Chemical Patents Inc. | Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace |
US7413648B2 (en) * | 2004-05-21 | 2008-08-19 | Exxonmobil Chemical Patents Inc. | Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking |
US7419584B2 (en) | 2004-05-21 | 2008-09-02 | Exxonmobil Chemical Patents Inc. | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
US7427381B2 (en) | 2004-05-21 | 2008-09-23 | Exxonmobil Chemical Patents Inc. | Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid |
US7431803B2 (en) | 2004-05-21 | 2008-10-07 | Exxonmobil Chemical Patents Inc. | Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks |
US7488459B2 (en) | 2004-05-21 | 2009-02-10 | Exxonmobil Chemical Patents Inc. | Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking |
US20060014993A1 (en) * | 2004-07-14 | 2006-01-19 | Stell Richard C | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US20060014992A1 (en) * | 2004-07-14 | 2006-01-19 | Stell Richard C | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US20080274023A1 (en) * | 2004-07-14 | 2008-11-06 | Stell Richard C | Process for Reducing Fouling from Flash/Separation Apparatus during Cracking of Hydrocarbon Feedstocks |
US7776286B2 (en) | 2004-07-14 | 2010-08-17 | Exxonmobil Chemical Patents Inc. | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US7408093B2 (en) | 2004-07-14 | 2008-08-05 | Exxonmobil Chemical Patents Inc. | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US7641870B2 (en) | 2004-07-14 | 2010-01-05 | Exxonmobil Chemical Patents Inc. | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US20080118416A1 (en) * | 2004-07-14 | 2008-05-22 | Stell Richard C | Process for Reducing Fouling From Flash/Separation Apparatus During Cracking of Hydrocarbon Feedstocks |
US7358413B2 (en) | 2004-07-14 | 2008-04-15 | Exxonmobil Chemical Patents Inc. | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US7285697B2 (en) | 2004-07-16 | 2007-10-23 | Exxonmobil Chemical Patents Inc. | Reduction of total sulfur in crude and condensate cracking |
US20060014994A1 (en) * | 2004-07-16 | 2006-01-19 | Keusenkothen Paul F | Reduction of total sulfur in crude and condensate cracking |
US20060094918A1 (en) * | 2004-10-28 | 2006-05-04 | Mccoy James N | Steam cracking of hydrocarbon feedstocks containing salt and/or particulate matter |
US7402237B2 (en) | 2004-10-28 | 2008-07-22 | Exxonmobil Chemical Patents Inc. | Steam cracking of hydrocarbon feedstocks containing salt and/or particulate matter |
US20060129012A1 (en) * | 2004-12-10 | 2006-06-15 | Frye James M | Vapor/liquid separation apparatus |
US7481871B2 (en) | 2004-12-10 | 2009-01-27 | Exxonmobil Chemical Patents Inc. | Vapor/liquid separation apparatus |
US20070004952A1 (en) * | 2005-06-30 | 2007-01-04 | Mccoy James N | Steam cracking of partially desalted hydrocarbon feedstocks |
US8173854B2 (en) | 2005-06-30 | 2012-05-08 | Exxonmobil Chemical Patents Inc. | Steam cracking of partially desalted hydrocarbon feedstocks |
US8118996B2 (en) | 2007-03-09 | 2012-02-21 | Exxonmobil Chemical Patents Inc. | Apparatus and process for cracking hydrocarbonaceous feed utilizing a pre-quenching oil containing crackable components |
US20090050530A1 (en) * | 2007-08-21 | 2009-02-26 | Spicer David B | Process and Apparatus for Steam Cracking Hydrocarbon Feedstocks |
US20100300936A1 (en) * | 2009-05-29 | 2010-12-02 | Stell Richard C | Method and Apparatus for Recycle of Knockout Drum Bottoms |
US8057663B2 (en) | 2009-05-29 | 2011-11-15 | Exxonmobil Chemical Patents Inc. | Method and apparatus for recycle of knockout drum bottoms |
US8435386B2 (en) | 2009-05-29 | 2013-05-07 | Exxonmobil Chemical Patents Inc. | Method and apparatus for recycle of knockout drum bottoms |
KR20200123476A (en) * | 2018-03-13 | 2020-10-29 | 루머스 테크놀로지 엘엘씨 | In-situ caulking of heavy pitches and other feedstocks with high fouling tendency |
Also Published As
Publication number | Publication date |
---|---|
NL6802193A (en) | 1968-08-26 |
DE1668674A1 (en) | 1972-02-17 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US3718709A (en) | Process for producing ethylene | |
CA1219005A (en) | Thermal cracking process for selectively producing olefins and aromatic hydrocarbons from hydrocarbons | |
US3030297A (en) | Hydrogenation of coal | |
US4587011A (en) | Thermal cracking process for selectively producing petrochemical products from hydrocarbons | |
JPS60219292A (en) | Selective production of petrochemicals | |
US2813916A (en) | Production of hydrocarbons from heavy hydrocarbonaceous residues by two stage processwith the use of inert solids | |
US3617514A (en) | Use of styrene reactor bottoms in delayed coking | |
US2207552A (en) | Manufacture of aromatic hydrocarbons from petroleum oil | |
US3641183A (en) | Injection of an electrically heated stream into a steam cracked product | |
US2951886A (en) | Recovery and purification of benzene | |
US2977299A (en) | Production of chemical products from coal products | |
US2245819A (en) | Process for the manufacture of ethylene | |
US2217250A (en) | Production of oil gas | |
US1940725A (en) | Process for treating carbonaceous material | |
US2364377A (en) | Process for the preparation of butadiene | |
US2572734A (en) | Production of carbon black from high-boiling aromatic oils or tars | |
US1847239A (en) | Process of treating hydrocarbons | |
Dunstan et al. | Symposium on Hydrocarbon Decomposition Thermal Treatment of Gaseous Hydrocarbons I. Laboratory Scale Operation | |
US4115208A (en) | Recovery of styrene from cracked hydrocarbon fractions | |
US2244636A (en) | Treatment of hydrocarbons | |
US2838584A (en) | Method of manufacturing acetylene from hydrocarbons | |
US2423374A (en) | Process for producing aromatics and diolefins from petroleum | |
US2086741A (en) | Method of converting hydrocarbon compounds | |
DE714487C (en) | Process for the production of anti-knock motor fuels | |
US2440492A (en) | Process for the production of diolefins |