US3881994A - Distillation column reboiler control system - Google Patents

Distillation column reboiler control system Download PDF

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Publication number
US3881994A
US3881994A US459975A US45997574A US3881994A US 3881994 A US3881994 A US 3881994A US 459975 A US459975 A US 459975A US 45997574 A US45997574 A US 45997574A US 3881994 A US3881994 A US 3881994A
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United States
Prior art keywords
reboiler
section
heater
flow
vapor
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Expired - Lifetime
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US459975A
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English (en)
Inventor
R Gene Fickel
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Honeywell UOP LLC
Universal Oil Products Co
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Universal Oil Products Co
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Publication date
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Priority to US459975A priority Critical patent/US3881994A/en
Priority to CA223,618A priority patent/CA1057222A/en
Priority to IN658/CAL/75A priority patent/IN145047B/en
Priority to DE19752515282 priority patent/DE2515282A1/de
Priority to ES436431A priority patent/ES436431A1/es
Priority to FR7511007A priority patent/FR2267134B1/fr
Priority to SU752125299A priority patent/SU591127A3/ru
Priority to IT22238/75A priority patent/IT1037220B/it
Priority to BR2799/75A priority patent/BR7502197A/pt
Priority to GB14733/75A priority patent/GB1500519A/en
Priority to JP50042865A priority patent/JPS50141577A/ja
Priority to PL1975179530A priority patent/PL102736B1/pl
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Publication of US3881994A publication Critical patent/US3881994A/en
Assigned to UOP, DES PLAINES, IL, A NY GENERAL PARTNERSHIP reassignment UOP, DES PLAINES, IL, A NY GENERAL PARTNERSHIP ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: KATALISTIKS INTERNATIONAL, INC., A CORP. OF MD
Assigned to UOP, A GENERAL PARTNERSHIP OF NY reassignment UOP, A GENERAL PARTNERSHIP OF NY ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: UOP INC.
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/42—Regulation; Control
    • B01D3/4211—Regulation; Control of columns
    • B01D3/4283—Bottom stream
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • ABSTRACT A control system for regulating the heat input to the reboiler section of a distillation (fractionation) column.
  • Flow-measuring means for determining the quantity of vapor, passing upwardly from the reboiler section into the fractionation section (stripping and rectification), and internally disposed within the reboiler section, provides a signal which is transmitted to the reboiler heater, thereby adjusting the fuel input thereto in order to regulate the degree of vaporization being effected therein.
  • the reboiler section" of the distillation column connotes that portion disposed below the lowermost tray, or deck. That portion of the column above the lowermost tray is herein referred to as the fractionation section,” and is inclusive of the rectification zone (above the feed tray) and the stripping zone (below the feed tray).
  • reboiling a distillation column connotes the circulation of a hot liquid bottoms fraction from the reboiler section through an external reboiler heater, wherein at least a portion of the liquid is vaporized; the heated, mixed-phase bottoms material is returned to the reboiler section.
  • the vapors pass upwardly from the reboiler section into the fractionation section wherein they serve to remove lower-boiling constituents from the liquid phase traversing the column in downward flow.
  • the latter constitutes the source of the greatest quantity of heat input to the reboiler section and, of necessity, must be subject to close control and- /or regulation. Additionally, the efficiency of separation, to obtain the desired product purity, is largely dependent upon the amount of vapor produced and the control thereof.
  • control system and method of the present invention is designed to achieve a constant rate of vapor production in the reboiler heater by adjusting, or regulating the flow of fuel to the heater in response to a signal which is representative of the actual quantity of vapor passing into the fractionation section of the distillation column.
  • a principal object of the present invention is to provide a method for measuring and controlling the vapors produced in the reboiler section of a distillation column.
  • a corollary objective is directed to a control system which is capable of constant heat input during steady-state operation.
  • my invention provides a control system for regulating the heat input to the reboiler section of a distillation column which comprises, in cooperative combination: (a) an inventory of liquid bottoms material contained in a suitable chamber in said reboiler section; (b) flow-regulating means for passing a portion of said liquid bottoms to a reboiler heater; (c) conduit means for passing heated, mixedphase bottoms material from said heater into said reboiler section; (d) fuel-varying means for adjusting the fuel input to said heater; (e) flow-measuring means for determining the quantity of vapor, in said mixed-phase bottoms material, passing from said reboiler section upwardly into the fractionation section of said distillation column, said flow-measuring means internally disposed within said reboiler section; and, (f) signal-receiving means for establishing a signal representative of the quantity of vapor passing into said fractionation section and for transmitting said signal to said fuel-varying means,
  • the ultimately recovered product has a relatively narrow boiling range, and its distillation characteristics are substantially similar to those of pure compounds.
  • my invention is most advantageously employed in situations where the column bottoms fraction, a portion of which serves as the circulating reboiler heating medium, is a pure compound, or a narrow boiling range mixture.
  • the basic reboiling technique is designed to provide the amount of vapor ous material required for thermal balance and separa tion efficiency by adjusting the quantity of fuel input to the reboiler heater, in order to regulate the heat input to the reboiler section of the distillation column.
  • control techniques involve controlling the flow of fuel medium to the reboiler heater in response either to the temperature of the heated material return to the reboiler section, or to the rate of mixed-phase flow.
  • the quantity of liquid reboiler bottoms material introduced into the reboiler heater must be pre-set by way of flow control means.
  • Flow control of the heated material reentering the reboiler section suffers from the disability of not being capable of precisely measuring vapor flow and depends upon, as an essential element, a constant flow rate to the heater.
  • Temperature control will generally suffice acceptably in situations where the reboiler liquid has a relatively wide boiling range, but fails miserably where it is either a substantially pure compound, or possesses a comparatively narrow boiling range, or where a relatively minor degree of vaporization is desired.
  • a most important criterion is the measurement of the degree of vaporization in the heated, mixed-phase material returning to the reboiler section of the column. This is especially critical with respect to substantially pure column bottoms material. Correlations of heat content versus temperature, at given vaporization percentages, indicate that a comparatively large delta-T exists per unit of heat content as the percentage vaporization increases in the case of a liquid bottoms material having a relatively wide boiling range. Thus, a measurable change in temperature will indicate a significant change in the degree of vaporization, and a corresponding change in the thermal balance of the column. Such changes can be employed to reset the flow of fuel medium to the heater so that more or less liquid will be vaporized and the Column can be held in close proximity to thermal equilibrium.
  • temperature control in the return conduit is not satisfactorily effective when the reboiler bottoms liquid is a substantially pure compound, or one having a narrow boiling range approximately F. or less.
  • the correlations described above indicate that very little (if any) delta-T is available for percent vaporization determination. That is to say, temperature measurement in any portion of either the reboiler heater circuit, or the lower reboiler section, does not indicate accurately the degree of vaporization achieved. The temperature will remain virtually the same whether excess vapor, or insufficient vapor, is being generated in the reboiler heater. It becomes, therefore, extremely difficult to maintain the distillation column at or near thermal equilibrium.
  • the control system of the present invention overcomes the deficiencies of prior art techniques, especially with respect to substantially pure compounds, or narrow boiling component mixtures. This is accomplished through the use of a novel reboiler section design which permits direct, internal measurement of the flow of generated vapor upwardly from the reboiler section to the fractionation section. A signal, representative of the quantity of vapor passing into the fractionation section is transmitted to fuel-varying means for adjustment, or regulation of the fuel input to the reboiler heater.
  • fuel-varying means for adjustment, or regulation of the fuel input to the reboiler heater.
  • An additional advantage resides in the fact that the lowest percentage vaporization, for a given set of operating variables, is capable of being maintained.
  • the internal measurement of the flow of vapors is extremely accurate and sensitive since it is accomplished within the reboiler section in a substantially liquid-free environment.
  • Examples of processes, wherein the separation and recovery of a pure compound, or narrow boiling range mixture forms an integral part, and to which the pres ent invention may be advantageously applied include, but not by way of limitation: (i) the recovery of styrene from an ethylbenzene dehydrogenation system; (ii) the separation of one xylene isomer from a mixture thereof with other xylene isomers; (iii) aromatic hydrocarbon separation from a mixture thereof with non-aromatic hydrocarbons; and, (iv) the separation and recovery of ethylbenzene from a mixture thereof with various xylene isomers, etc.
  • the particular use, to which the present invention is put, is not to be considered a feature limiting upon the scope and spirit thereof as defined by the appended claims.
  • Extractive distillation conditions include a solvent water content of about 0.5 to 20.0 percent by weight, a solvent to hydrocarbon feed ratio of about 2.0: 1.0 to 60:10, a distillation column pressure ranging from 90 mm.
  • Hg absolute, to about 40.0 psig., an overhead temperature from 130 to about 330F. and a reboiler bottoms temperature from 170 to about 355F.
  • a liquid extract bottoms stream relatively free from nonaromatics and comprising solvent and aromatic hydrocarbons
  • an overhead vaporous raffinate comprising non-aromatics, water (as steam) and a relatively minor quantity of the sulfolane solvent.
  • the raffinate is condensed and water-washed to recover substantially solvent-free non-aromatic hydrocarbons contained in the extract phase are recovered in a solvent recovery column of the variety well known and thoroughly described in the prior art.
  • Aromatic hydrocarbon recovery generally exceeds 96.5 percent by volume, based upon the charge stock, and the aromatic purity is greater than 99.0 percent.
  • Extractive distillation column I is shown as having a fractionation section 4 located above the lowermost tray 6, and a reboiler section 4a located below tray 6.
  • Reboiler section 4a is partitioned by chordal baffle 9 to provide two liquid inventory chambers 9a and 9b.
  • the solvent to feed mol ratio approximates 30:10, and the hydrocarbon feed is introduced via line 2.
  • Operating pressures include a reboiler section pressure of about l7.0 psig., a pressure of about 12.0 psig. at the locus of hydrocarbon feed and a top pressure of about 7.0 psig.
  • the reboiler section temperature is about 350F. and the vaporous raffinate overhead stream, in line 5, is at a temperature of about 285F.
  • Distillation column 1 is shown as having an upper fractionation section 4 which, for the purposes of the present illustration, includes all trays above tray 6, or both the stripping and rectification sections. That portion of column 1 below tray 6 is herein referred to as the reboiler section. Located entirely within reboiler section 4a, is flow-measuring means generally indicated as 7. Flow-measuring means 7 is formed, in part, by chordal baffle 9 which terminates a finite distance below tray 6, and extends downwardly through reboiler section 4a, being immovably connected to the internal surface of the bottom head of column 1. There is provided, thereby, two liquid inventory chambers and 9b, and, in combination with partition 10, there is formed a riser 11.
  • an orifice plate is placed in riser 11 which supplies the flow-measuring means to determine the quantity of vaporous material passing therethrough into fractionation section 4.
  • a riser cap 8 is also provided in order to prevent liquid material from tray 6 from entering riser-orifice 11.
  • the flow-measuring means can take the form of a venturi.
  • the essential feature resides in the internal measurement of vapor flow into the fractionation section, and preferably in a substantially liquid-free environment. Thus, all the liquid material passing downwardly from tray 6 is collected in liquid inventory chamber 9b.
  • Flow-Recorder-Controller (FRC) 13 which receives a signal, via line 12, representative of the quantity of vapors passing upwardly through riser-orifice 1], is pre-set to transmit the signal via line 14 to fuelvarying means 15.
  • FRC 13 is set to provide the minimum quantity of vapors, passing upwardly into fractionation section 40. If an insufficient quantity of stripping vapors are supplied by reboiler heater l7, non-aromatic hydrocarbons will appear in the liquid bottoms product; conversely, an excess quantity of vapors will, in effect, throw" solvent and/or aromatics into the nonaromatic raffinate overhead. In either situation, the resulting upset in thermal balance adversely affects the desired separation efficiency of the distillation column. Only through the use of the present invention, wherein the vapor flow is internally measured, can controlled, steady-state operation be maintained.
  • feed composition aromatic/non-aromatic ratio
  • hydrocarbon charge stock rate varying hydrocarbon charge stock rate
  • solvent- /feed mol ratio a change in the solvent- /feed mol ratio.
  • other operating variables such as temperature, pressure, reflux rate (if any), water content of the solvent, desired product state, etc., affect thermal balance, but not to as great a degree.
  • Reboiler liquid is withdrawn from inventory chamber 9b in response to Level-Recorder-Controller (LRC) 28 which senses the level of liquid bottoms therein via conduits 29 and 30.
  • LRC 28 transmits a signal to FRC 32 via line 31, reset the set-point thereof.
  • FRC 32 senses, via line 33 and orifice 36, the flow of liquid through conduit 37, and makes the necessary adjustment in control valve 35.
  • the amount of liquid bottoms material, at a temperature approximating 3 l2F., flowing through conduit 37 into heater 17, is about 4,381 mols/hr.
  • Sufficient fuel is supplied to heater 17, through line 16, to produce a heated mixed-phase fluid, in line 38, having a temperature of about 350F.
  • the mixed-phase is reintroduced into reboiler section 4a through inlet port 39.
  • inventory chamber 90 a phase separation takes place to the extent that 1,164 mols/hr. of vapor pass upwardly ough the riser-orifice 11, into the fractionation section.
  • the 3,217 mols/hr. ofliquid are withdrawn by way of conduit 27, and transported thereby to a solvent re covery system not illustrated in the drawing.
  • Level-lndicating-Controller l8 senses the liquid level in inventory chamber 9a by way of conduits l9 and 20. Its principal function is to maintain a liquid seal at the bottom of the inventory chamber, while simultaneously maintaining the liquid level out of contact with the riser-orifice. A signal is transmitted by way of line 21 to FRC 22, to re-set the set point thereof. FRC 22 senses the flow ofliquid through line 27 via conduit 25 and orifice 26, and accordingly adjusts, via line 23, the flow through control valve 24.
  • LIC 18 senses an increasing liquid level in inventory chamber 9a.
  • the resulting transmitted signal causes control valve 24 to open wider, thereby sending the additional liquid bottoms to the solvent recovery facility.
  • cascade-type control loops represented (l by LRC 28, FRC 32 and control valve 35, and (2) MC 18, FRC' 22 and control valve 24, are not essential to my invention. They are illustrated as preferred instrumentation techniques to achieve smoother functioning in the operation thereof Likewise, reboiler heater 17 may take the form of a tube and shell heat-exchanger, or a direct-fired heater as illustrated.
  • a control system for regulating the heat input to the reboiler section ofa distillation column which comprises, in cooperative combination:
  • a reboiler heater having feed input means thereto connected to said chamber, flow regulating means for controlling the flow of said liquid bottoms from said chamber to said reboiler heater in accordance with the liquid level in said chamber;
  • conduit means in interconnection with said reboiler heater for passing heated, mixed'phase bottoms material from said heater into a partitioned and segregated portion of said chamber in said reboiler section;
  • vapor flow-measuring means in said reboiler section responsive to the total quantity of upward flowing vapor from said mixed-phase bottoms ma terial passing from said segregated portion of said reboiler section upwardly into the fractionation section of said distillation column, said flow measuring means being internally disposed within said segregated portion of said reboiler section;
  • signal-generating means in said segregated portion of said reboiler section for establishing a signal representative of the volumetric flow rate of vapor from said segregated portion passing into said fractionation section, and signal transmitting means for modifying and transmitting the resulting signal to said fuel varying means, whereby fuel input through said fuel input means to said heater is decreased in response to increasing flow rates of said vapor and increased in response to decreasing flow rates of said vapor;
  • said control system being fur ther characterized in that said reboiler section is partitioned to provide two inventory chambers of said liquid bottoms material, the first of which is said segregated portion which has said vapor flow measuring means disposed therein and the second of which is connected to said freed input means.
  • control system of claim 1 further characterized in that a second flow-regulating means effects withdrawal of bottoms material from the first of said inventory chambers and out of said distillation column.
  • control system of claim 2 further characterized in that said second flow-regulating means, includes means to maintain the level of the liquid bottoms in said first inventory chamber out of contact with said flow-measuring means.
  • a method for controlling the heat input to the reboiler section of a distillation column, in response to variations in the steady-state operation of said column comprises the steps of:

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US459975A 1974-04-11 1974-04-11 Distillation column reboiler control system Expired - Lifetime US3881994A (en)

Priority Applications (12)

Application Number Priority Date Filing Date Title
US459975A US3881994A (en) 1974-04-11 1974-04-11 Distillation column reboiler control system
CA223,618A CA1057222A (en) 1974-04-11 1975-04-02 Distillation column reboiler control system
IN658/CAL/75A IN145047B (enrdf_load_stackoverflow) 1974-04-11 1975-04-02
DE19752515282 DE2515282A1 (de) 1974-04-11 1975-04-08 Verfahren und einrichtung zum regeln und/oder steuern der waermeeingabe in einen aufwaermerabschnitt einer destillationssaeule
FR7511007A FR2267134B1 (enrdf_load_stackoverflow) 1974-04-11 1975-04-09
ES436431A ES436431A1 (es) 1974-04-11 1975-04-09 Un sistema de control para regular la entrada de calor a la seccion de rehervidor de una columna de destilacion.
SU752125299A SU591127A3 (ru) 1974-04-11 1975-04-10 Устройство дл регулировани теплоподвода к секции кип тильника перегонной колонны
IT22238/75A IT1037220B (it) 1974-04-11 1975-04-10 Impianto e procedimento per il controllo della cessione di calore ad una colonna di distillazione
BR2799/75A BR7502197A (pt) 1974-04-11 1975-04-10 Dispositivo e processo de controle para regular a admissao de calor a uma secao de refervedor
GB14733/75A GB1500519A (en) 1974-04-11 1975-04-10 Distillation column reboiler control system
JP50042865A JPS50141577A (enrdf_load_stackoverflow) 1974-04-11 1975-04-10
PL1975179530A PL102736B1 (pl) 1974-04-11 1975-04-11 Sposob regulacji ilosci ciepla doprowadzanego do sekcji ponownego odparowania w kolumnie destylacyjnej i uklad do regulacji ilosci ciepla doprowadzanego do sekcji ponownego odparowania w kolumnie destylacyjnej

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US459975A US3881994A (en) 1974-04-11 1974-04-11 Distillation column reboiler control system

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US3881994A true US3881994A (en) 1975-05-06

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US459975A Expired - Lifetime US3881994A (en) 1974-04-11 1974-04-11 Distillation column reboiler control system

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US (1) US3881994A (enrdf_load_stackoverflow)
JP (1) JPS50141577A (enrdf_load_stackoverflow)
BR (1) BR7502197A (enrdf_load_stackoverflow)
CA (1) CA1057222A (enrdf_load_stackoverflow)
DE (1) DE2515282A1 (enrdf_load_stackoverflow)
ES (1) ES436431A1 (enrdf_load_stackoverflow)
FR (1) FR2267134B1 (enrdf_load_stackoverflow)
GB (1) GB1500519A (enrdf_load_stackoverflow)
IN (1) IN145047B (enrdf_load_stackoverflow)
IT (1) IT1037220B (enrdf_load_stackoverflow)
PL (1) PL102736B1 (enrdf_load_stackoverflow)
SU (1) SU591127A3 (enrdf_load_stackoverflow)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3964975A (en) * 1974-08-19 1976-06-22 Texaco Inc. Means for controlling the temperature of a depropanizer tower
US4046638A (en) * 1975-06-12 1977-09-06 Uop Inc. Method for controlling heat input to the reboiler section of a distillation column
EP0005138A1 (en) * 1978-04-28 1979-11-14 Texaco Development Corporation Process for producing synthesis gas with wash water purification and novel flash column for use in said process
US4501657A (en) * 1983-02-01 1985-02-26 Phillips Petroleum Company Preheating of distillation feed
EP0133510A1 (de) * 1983-08-03 1985-02-27 BASF Aktiengesellschaft Verfahren zur destillativen Zerlegung eines azeotropen Stoffgemisches
GB2193110A (en) * 1986-08-02 1988-02-03 Lucas Ind Plc Solvent cleaning apparatus
EP0364659A1 (en) * 1988-10-21 1990-04-25 Nkk Corporation Method for rectification and apparatus therefor
US5205909A (en) * 1991-12-04 1993-04-27 Union Carbide Chemicals & Plastics Technology Corporation Apparatus for measuring reflux flow in a distillation column
WO2000025881A1 (de) * 1998-10-29 2000-05-11 Krupp Uhde Gmbh Rektifizierkolonne für die extraktivdestillation von eng- oder azeotrop siedenden gemischen
CN100418601C (zh) * 2006-03-21 2008-09-17 浙江工业大学 一种精馏塔内回流控制装置
CN102000449A (zh) * 2009-09-02 2011-04-06 美国Gtc技术有限责任公司 通过向再沸器添加蒸汽以改善萃取蒸馏的方法和设备
US20130078115A1 (en) * 2010-06-11 2013-03-28 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for drying and compressing a co2-rich stream
WO2021219933A1 (en) * 2020-04-27 2021-11-04 Chempolis Oy Heteroazeotropic extractive distillation method and apparatus

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4003799A (en) * 1975-06-12 1977-01-18 Uop Inc. Method for controlling heat input to the reboiler section of a distillation column
DE2916175A1 (de) * 1979-04-21 1980-10-23 Krupp Koppers Gmbh Verfahren zur regelung der einer extraktivdestillationskolonne am sumpf zugefuehrten waermemenge

Citations (5)

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Publication number Priority date Publication date Assignee Title
US3225550A (en) * 1963-03-04 1965-12-28 Phillips Petroleum Co Fractional distillation control system
US3411308A (en) * 1967-01-03 1968-11-19 Phillips Petroleum Co Method and apparatus for controlling by a material balance the bottoms flow rate in a fractional distillation system
US3442767A (en) * 1968-05-16 1969-05-06 Sinclair Research Inc Stripping operation without overhead reflux and the control of the water content in the system
US3766021A (en) * 1971-05-03 1973-10-16 Phillips Petroleum Co Process and apparatus for fractionator reboiling with minimized fouling by centifuging and decanting
US3803002A (en) * 1971-07-23 1974-04-09 Phillips Petroleum Co Method and apparatus for controlling the operating of a fractionator

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3225550A (en) * 1963-03-04 1965-12-28 Phillips Petroleum Co Fractional distillation control system
US3411308A (en) * 1967-01-03 1968-11-19 Phillips Petroleum Co Method and apparatus for controlling by a material balance the bottoms flow rate in a fractional distillation system
US3442767A (en) * 1968-05-16 1969-05-06 Sinclair Research Inc Stripping operation without overhead reflux and the control of the water content in the system
US3766021A (en) * 1971-05-03 1973-10-16 Phillips Petroleum Co Process and apparatus for fractionator reboiling with minimized fouling by centifuging and decanting
US3803002A (en) * 1971-07-23 1974-04-09 Phillips Petroleum Co Method and apparatus for controlling the operating of a fractionator

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3964975A (en) * 1974-08-19 1976-06-22 Texaco Inc. Means for controlling the temperature of a depropanizer tower
US4046638A (en) * 1975-06-12 1977-09-06 Uop Inc. Method for controlling heat input to the reboiler section of a distillation column
EP0005138A1 (en) * 1978-04-28 1979-11-14 Texaco Development Corporation Process for producing synthesis gas with wash water purification and novel flash column for use in said process
US4501657A (en) * 1983-02-01 1985-02-26 Phillips Petroleum Company Preheating of distillation feed
EP0133510A1 (de) * 1983-08-03 1985-02-27 BASF Aktiengesellschaft Verfahren zur destillativen Zerlegung eines azeotropen Stoffgemisches
GB2193110A (en) * 1986-08-02 1988-02-03 Lucas Ind Plc Solvent cleaning apparatus
GB2193110B (en) * 1986-08-02 1990-07-18 Lucas Ind Plc Solvent cleaning apparatus
EP0364659A1 (en) * 1988-10-21 1990-04-25 Nkk Corporation Method for rectification and apparatus therefor
US5205909A (en) * 1991-12-04 1993-04-27 Union Carbide Chemicals & Plastics Technology Corporation Apparatus for measuring reflux flow in a distillation column
US5314587A (en) * 1991-12-04 1994-05-24 Union Carbide Chemicals & Plastics Technology Corporation Method for measuring reflux flow in a distillation process
WO2000025881A1 (de) * 1998-10-29 2000-05-11 Krupp Uhde Gmbh Rektifizierkolonne für die extraktivdestillation von eng- oder azeotrop siedenden gemischen
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GB1500519A (en) 1978-02-08
FR2267134A1 (enrdf_load_stackoverflow) 1975-11-07
FR2267134B1 (enrdf_load_stackoverflow) 1979-06-01
BR7502197A (pt) 1976-02-10
IT1037220B (it) 1979-11-10
JPS50141577A (enrdf_load_stackoverflow) 1975-11-14
CA1057222A (en) 1979-06-26
SU591127A3 (ru) 1978-01-30
IN145047B (enrdf_load_stackoverflow) 1978-08-19
ES436431A1 (es) 1977-01-01
PL102736B1 (pl) 1979-04-30
DE2515282A1 (de) 1975-10-16

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