US3103485A - Temperature - Google Patents

Temperature Download PDF

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Publication number
US3103485A
US3103485A US841660A US3103485A US 3103485 A US3103485 A US 3103485A US 841660 A US841660 A US 841660A US 3103485 A US3103485 A US 3103485A
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Prior art keywords
quench
cracking
percent
range
olefins
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Priority to NL260717D priority Critical patent/NL260717A/xx
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Priority to US841660 priority patent/US3103485A/en
Priority to GB826/61A priority patent/GB944758A/en
Priority to DEE20523A priority patent/DE1294366B/de
Application granted granted Critical
Publication of US3103485A publication Critical patent/US3103485A/en
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S261/00—Gas and liquid contact apparatus
    • Y10S261/54—Venturi scrubbers

Definitions

  • the mixed product obtained is highly compatible and can be easily separated by simple distillation.
  • the polymer produced in the conventional high conversioncracking process would contaminate the C 5C g straight chain olefins produced in thewax cracking operation.
  • the boiling range andex-tent of the formation of this polymer is such that these C C olefins may be separated by simpleidistillation with little contamination by polymeric-materials formed in the light naphtha cracking operation.
  • a cracking furnace 3 This furnace is operated at estates parafiinic stock which is pourand cloud point of the middle temperatures of 1300 to 1500 F., preferably 1380 to 1450 F., e.g. 1400 F., pressures of to 50 p.s.i.g., preferably to 25 p.s.i.g., e.g. p.s.i.g., with residence times of 0.1 to 5, preferably 0.5 to 2, e.g. 1 second and with amounts of steam supplied being in the range of 0.1 to 1, preferably 0.2 to 0.5, e.g. 0.25 lb.
  • a waxy distillate quench oil is supplied through line 6 to quench the efiiuent from the cracking zone which is passed through line 4 to quench zone 5.
  • This quench zone maybe an elongated tube with provision for multiple or alternate injection of the waxy distillate oil through lines 7, S, 9, 10, 11, 1 2, 13, and 14 in addition to line 6, if. desired, as the vapors pass through the tube.
  • the quenched products from the cracking of the light naphtha feed and from the low conversion cracking of the waxy distillate are passed from the quench zone 5 through line 15 to further quench facilities and of course, fractionation facilities for separation of theproducts.
  • feedstocks are extracted gas oils (to remove some of the aromatics and naphthenes) and the raflinate from the extraction of catalytic cracking unit cycle stocks boiling in the range of 650 to 900 t P. All of the materials above described will produce high yields of the desired. C to C linear olefins.
  • quenching may be conducted by supplying quench oil at multiple points in stages through the quench zone or may be conducted by supplying the entire amount of the quench oil. initially. It should be noted that it may be preferred to introduce the major portion of the quench oil initially so as to quickly reduce the temperature to say 1200 to 1 300 F.,
  • .water may be supplied through lines 6- to 14 for additional control of temperature and that steam may be supplied at the beginning of the zone through line 6 to control the proportion of steam to hydrocarbon in the quench zone if desired.
  • the waxy distillate oil may be introduced at temperatures of 400 to-800 F., preferably 500 to 700 F., e.g. 600 F. and supplied in amounts based on the gaseous efliuent (including H O) of 30' to 70 wt.
  • Quenching times may be in the range of 0.2 to 2 seconds preferably 0.2 to 1, e.g. 0.5 second (i.e. time to reduce the temperature to below about 1000 F.)
  • the 1000 F. eflluent is passed to a conventional steam cracker quench tower wherein the original steam cracker product and the additional product from the wax cracking are separated by conventional fractionation means.
  • the light products (C and lighter) are removed overhead as a gas to be processed further in a conventional light ends system.
  • Steam cracked naphtha (300 F. End Point or so) is also removed overhead, as a liquid, and is sent to the same light ends system, and/or conventional naphtha fractionation and finally char treating.
  • the heavier steam cracked products, as well as recycle quench oil are removed as sidestneams and bottoms streams from said quench tower.
  • a commercial high conversion steam cracker is operated under conventional furnace efiiuent conditions.
  • a waxy distillate preheated to 600 F., is used as the quench material in a system as described in the drawing, (FIG. 1).
  • Sufficient waxy distillate is injected into the cracker efli uent to cool it from 1400 to 1000 F.
  • a residence time of e.g. 0.5 second isutilized in the quench line, with uniform addition of quench material to the flowing gas 1 stream along the length of the line.
  • the result obtained is similar to that obtained in a conventional quench utilizing a single injection point at the inlet.
  • Wax feed temperature 800 F. Coil-outlet temperature 1,100 Residence time 1 sec;
  • the pour of the 600 to 800 F. product must be 55 F.
  • the 610+ F. product was 63-66% of feed.
  • Example 'In a system as described in FIGURE I a light naphtha boiling in the range of 160220 F. is cracked under the following conditions:
  • ploymer in ur- 1 range 628 1-b./-hr.
  • percent C3 conversion refers to the percent by weight of C gases obtained per weight of naphtha cracked.
  • An improved process for preparing predominantly straight chain olefins in the C to C range along with olefins and diolefins boiling in the C to G range which comprises cracking a light naphtha in a cracking zone in the presence of steam at temperatures in the range of 1300 to 1500 F. and under conditions to obtain conversions (to C of above 40 wt. percent, withdrawing the product vapors from said cracking zone, immediately contacting the withdrawn product vapors, with 30 to 70 wt. percent of a waxy distillate based on the product vapors thereby quenching said product vapors to below about 0 F. in from 0.2 to 2 seconds and also obtaining the major proportion of the waxy distillate cracking at about 1100 F. and separating a out high in C to C olefins and a cut high in C to C olefins and diolefins from the resultant mixture.
  • waxy distillate is a virgin gas oil boiling in the range of 500 to 1200 F.
  • waxy distillate is a petrolatum boiling in the range of 650 to 1100 F.
  • quenching is conducted by supplying the quench oil at multiple points through a staged quench zone.
  • An improved process for preparing a fraction con taining a high proportion of straight chain and minimum branched chain olefins in the C to C range along With olefins and diolefins boiling in the C to C range which comprises cracking a light naphtha in a cracking zone in the presence of steam at temperatures in the range of 1300 to 1500" F. under conditions to obtain C conversions of above 40 wt. percent and utilizing amounts of steam supplied in' the range of 0.2 to 0.5 lb. of steam per lb. of oil and residence times of 0.5 to 2 seconds, immediately quenching in a quench zone the product vapors from said cracking'zon'e with 40 to 60 Wt.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US841660 1960-02-12 1960-02-12 Temperature Expired - Lifetime US3103485A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
NL260717D NL260717A (enrdf_load_stackoverflow) 1960-02-12
US841660 US3103485A (en) 1960-02-12 1960-02-12 Temperature
GB826/61A GB944758A (en) 1960-02-12 1961-01-09 Cracking waxy distillates
DEE20523A DE1294366B (de) 1960-02-12 1961-01-28 Verfahren zur thermischen Spaltung von Kohlenwasserstoffen

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US841660 US3103485A (en) 1960-02-12 1960-02-12 Temperature

Publications (1)

Publication Number Publication Date
US3103485A true US3103485A (en) 1963-09-10

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ID=21731475

Family Applications (1)

Application Number Title Priority Date Filing Date
US841660 Expired - Lifetime US3103485A (en) 1960-02-12 1960-02-12 Temperature

Country Status (4)

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US (1) US3103485A (enrdf_load_stackoverflow)
DE (1) DE1294366B (enrdf_load_stackoverflow)
GB (1) GB944758A (enrdf_load_stackoverflow)
NL (1) NL260717A (enrdf_load_stackoverflow)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3346498A (en) * 1966-06-06 1967-10-10 Chevron Res Lubricating oiil composition containing high molecular weight olefin-diolefin copolymer
US3705926A (en) * 1970-02-20 1972-12-12 Paul Rumpf Manufacture of long chain alpha-olefines from mixtures of heavy paraffins
US3718709A (en) * 1967-02-23 1973-02-27 Sir Soc Italiana Resine Spa Process for producing ethylene
US3928173A (en) * 1974-05-21 1975-12-23 Phillips Petroleum Co Increased production of diesel oil and fuel oil
US4021501A (en) * 1974-08-28 1977-05-03 Imperial Chemical Industries Limited Production of hydrocarbons
US4042488A (en) * 1973-10-31 1977-08-16 Texaco Inc. Thermal cracking wax to normal alpha-olefins
US4168224A (en) * 1977-02-14 1979-09-18 The Standard Oil Company (Ohio) Coking drum and process for forming improved graphite coke
US5092981A (en) * 1986-02-19 1992-03-03 Gaetano Russo Process for quenching hydrocarbon cracking apparatus effluent
US5136118A (en) * 1990-08-23 1992-08-04 Mobil Oil Corporation High VI synthetic lubricants from cracked refined wax
US5146022A (en) * 1990-08-23 1992-09-08 Mobil Oil Corporation High VI synthetic lubricants from cracked slack wax
US5208403A (en) * 1992-01-09 1993-05-04 Mobil Oil Corporation High VI lubricant blends from slack wax
US5324486A (en) * 1986-02-02 1994-06-28 Gaetano Russo Hydrocarbon cracking apparatus
US20080221378A1 (en) * 2007-03-09 2008-09-11 Stell Richard C Apparatus and Process for Cracking Hydrocarbonaceous Feed Utilizing a Pre-Quenching Oil Containing Crackable Components

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2731508A (en) * 1951-06-08 1956-01-17 Exxon Research Engineering Co Conversion of hydrocarbons for the production of unsaturates and gasoline with the use of inert solids
US2736685A (en) * 1953-01-02 1956-02-28 Exxon Research Engineering Co Process of petrolatum cracking in liquid and vapor phase
US2786802A (en) * 1955-08-17 1957-03-26 Kellogg M W Co Separation of steam and hydrocarbons
US2951029A (en) * 1958-06-09 1960-08-30 Exxon Research Engineering Co Naphtha steam-cracking quench

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE160519C (enrdf_load_stackoverflow) *
DE753849C (de) * 1935-11-01 1951-11-08 Bataafsche Petroleum Verfahren zum Herstellen hoehermolekularer Olefine durch Spalten von paraffinhaltigen Kohlenwasserstoffgemischen in der Dampfphase
US2172228A (en) * 1935-11-01 1939-09-05 Shell Dev Process for the manufacture of olefins
DE938844C (de) * 1951-06-08 1956-02-09 Standard Oil Dev Co Verfahren zur Umwandlung von Kohlenwasserstoff-Rueckstandsoelen
DE1076666B (de) * 1953-01-02 1960-03-03 Exxon Research Engineering Co Verfahren zur Crackung von Vaseline zur Gewinnung moeglichst hoher Ausbeuten an C- bis C-ª‡-Olefinen
DE1045388B (de) * 1953-06-22 1958-12-04 Exxon Research Engineering Co Verfahren zur Abtrennung gasfoermiger Kohlenwasserstoffe mit 1 bis 4 Kohlenstoffatomen aus einem gasfoermigen Gemisch, das bei der Fraktionierung von Produkten einer Hochtemperaturcrackung von Kohlenwasserstoffoelen anfaellt
FR1136012A (fr) * 1955-09-13 1957-05-07 Exxon Research Engineering Co Procédé de craquage du pétrolatum en phase liquide et vapeur

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2731508A (en) * 1951-06-08 1956-01-17 Exxon Research Engineering Co Conversion of hydrocarbons for the production of unsaturates and gasoline with the use of inert solids
US2736685A (en) * 1953-01-02 1956-02-28 Exxon Research Engineering Co Process of petrolatum cracking in liquid and vapor phase
US2786802A (en) * 1955-08-17 1957-03-26 Kellogg M W Co Separation of steam and hydrocarbons
US2951029A (en) * 1958-06-09 1960-08-30 Exxon Research Engineering Co Naphtha steam-cracking quench

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3346498A (en) * 1966-06-06 1967-10-10 Chevron Res Lubricating oiil composition containing high molecular weight olefin-diolefin copolymer
US3718709A (en) * 1967-02-23 1973-02-27 Sir Soc Italiana Resine Spa Process for producing ethylene
US3705926A (en) * 1970-02-20 1972-12-12 Paul Rumpf Manufacture of long chain alpha-olefines from mixtures of heavy paraffins
US4042488A (en) * 1973-10-31 1977-08-16 Texaco Inc. Thermal cracking wax to normal alpha-olefins
US3928173A (en) * 1974-05-21 1975-12-23 Phillips Petroleum Co Increased production of diesel oil and fuel oil
US4021501A (en) * 1974-08-28 1977-05-03 Imperial Chemical Industries Limited Production of hydrocarbons
US4168224A (en) * 1977-02-14 1979-09-18 The Standard Oil Company (Ohio) Coking drum and process for forming improved graphite coke
US5324486A (en) * 1986-02-02 1994-06-28 Gaetano Russo Hydrocarbon cracking apparatus
US5092981A (en) * 1986-02-19 1992-03-03 Gaetano Russo Process for quenching hydrocarbon cracking apparatus effluent
US5136118A (en) * 1990-08-23 1992-08-04 Mobil Oil Corporation High VI synthetic lubricants from cracked refined wax
US5146022A (en) * 1990-08-23 1992-09-08 Mobil Oil Corporation High VI synthetic lubricants from cracked slack wax
US5276229A (en) * 1990-08-23 1994-01-04 Mobil Oil Corp. High VI synthetic lubricants from thermally cracked slack wax
US5208403A (en) * 1992-01-09 1993-05-04 Mobil Oil Corporation High VI lubricant blends from slack wax
US20080221378A1 (en) * 2007-03-09 2008-09-11 Stell Richard C Apparatus and Process for Cracking Hydrocarbonaceous Feed Utilizing a Pre-Quenching Oil Containing Crackable Components
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

Also Published As

Publication number Publication date
GB944758A (en) 1963-12-18
NL260717A (enrdf_load_stackoverflow)
DE1294366B (de) 1969-05-08

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