CS252961B1

CS252961B1 - A method of treating waste gases from gasoline production and a scaffolding machine

Info

Publication number: CS252961B1
Application number: CS858440A
Authority: CS
Inventors: Jaroslav Klatik; Vladimir Klempa; Pavol Omyliak; Zdeno Uhlik
Original assignee: Jaroslav Klatik; Vladimir Klempa; Pavol Omyliak; Zdeno Uhlik
Priority date: 1985-11-22
Filing date: 1985-11-22
Publication date: 1987-10-15
Also published as: CS844085A1

Abstract

Sposob spracovania odpadových plynov z výroby benzínov a zariadenie k vykonávaniu tohto spósobu, pri ktorom sa získaný uhíovodíkový kondenzát po ochladení plynov v kondenzátore používá ako zložka automobilových a technických benzínov alebo vo formě suroviny pre pyrolýzu, pričom neskondenzované plyny sa po ohriatí v splyňovači spalujú v plynových horákoch techno'ogickej pece. Pri nedostatočnom množstve odpadových plynov a znížení tlaku v odplynovom systéme pod 15 až 30 kPa sa do rozvodu plynu privádza rafinérsky vykurovací plyn a pri ďalšom znížení tlaku pod 10 až 15 kPa zemný plyn. Pri přebytku odpadových plynov a zvýšení tlaku v odplynovom systéme nad 30 až 60 kPa sa odpadové plyny spalujú na pofnom horáku.A method for processing waste gases from gasoline production and a device for carrying out this method, in which the obtained hydrocarbon condensate after cooling the gases in a condenser is used as a component of automotive and technical gasolines or in the form of raw material for pyrolysis, while the uncondensed gases are burned in gas burners of a technological furnace after heating in a gasifier. In the case of an insufficient amount of waste gases and a decrease in the pressure in the exhaust gas system below 15 to 30 kPa, refinery heating gas is fed into the gas distribution system, and in the case of a further decrease in the pressure below 10 to 15 kPa, natural gas. In the case of an excess of waste gases and an increase in the pressure in the exhaust gas system above 30 to 60 kPa, the waste gases are burned in a furnace burner.

Description

3 4 2529613, 4, 252961

Vynález sa týká spůsobu spracovanla od-padových plynov z výroby benzínov, z redes-tilácie reformátu a ťažkého benzínu, z kom-plexu zariadení na reformovanie benzínov azo zariadení na hydrogenačnú rafináciu pa-liv a zariadenia na vykonávanie tohto spo-sobu.BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a process for treating waste gas from gasoline production, reformat reforming and naphtha, from gasoline reformer complexes, and from fuels hydrotreating plants and apparatus.

Doteraz známe riešenia používajú na za-chytenie a opatovné využitie odpadovýchplynov z výroby benzínov vo formě palivakompresory alebo spdsob priameho prepo-jenia p’ynov bez obsahu ťažších zložiek, naj-ma uhfovodíkov Cs, Ce, do horákov tech-nologických pecí.So far known solutions have been used for the recovery and utilization of waste gases from gasoline production in the form of a fuel compressor or a method for direct conversion of heavier-free p-yns into the furnace burners.

Nevýhodou týchto riešení sú relativné vy-soké investičné a prevádzkové náklady, niž-šia účinnosť zachytenia a spracovania od-padových plynov a v súvislosti s vysokýmobsahom ťažších zložiek v odpadových ply-noch z výroby benzínov potřeba účinnéhoodlúčenia týchto zložiek ešte před kompre-sům plynov. Odpadové plyny s obsahom ťaž-ších zložiek nie je možné priamo prepojiťdo plynových horákov z dovodu kondenzá-cie týchto zložiek a sposobovania ťažkostípri ich spalovaní.The disadvantage of these solutions is the relatively high investment and operating costs, the lower efficiency of the collection and treatment of waste gases and the need for efficient separation of these components prior to gas compression in connection with the high content of heavier constituents in gasoline off-gases. The waste gases containing the heavier components cannot be directly coupled to the gas burners due to the condensation of these components and the operation of the incinerators.

Uvedené nevýhody súčasného stavu tech-niky sú odstraněné sposobom spracovaniaodpadových plynov z výroby benzínov po-dlá vynálezu, ktorého podstata spočívá vtom, že odpadové plyny sú chladené na tep-lotu 5 až 30 °C, s výhodou 15 °C, pričom do-chádza k vykondenzovaniu uhfovodíkov Cs,Ce, ktoré sú odvádzané priamo do finálnychrafinérskych produktov, motorových paív,technických benzínov alebo sa použijú akosurovina pre pyrolýzu. Ďalej je podstatouvynálezu to, že rteskondenzované plyny súohrievané na teplotu 50 až 100 °C, s výho-dou 70 °C, aby nastalo úplné splynenie uh-1'ovodíkov Cs, pričom po redukcii tlaku na2 až 10 kPa sú odpadové plyny spalovanév plynových horákoch a v případe zvýše-nia tlaku v odplynovom systéme nad 30 až60 kPa sú spalované na pofnom horáku a vpřípade zníženia tlaku v odplynovom systé-me pod 15 až 30 kPa je privádzaný do ply-nových horákov rafinérsky vykurovací plyn,pričom pri ďalšom znížení tlaku v odplyno-vom systéme pod 10 až 15 kPa je privádzanýdo plynových horákov zemný plyn ako sta-bilný zdroj plynného paliva. Výhodou sposobu spracovania odpadovýchplynov z výroby benzínov podTa vynálezu jemožnost spracovania aj tých odpadovýchplynov, ktoré obsahujú ťažšie zložky, najmáuhlovodíky Cs, Ce a to kvapalného uhlovo-díkového kondenzátu ako komponentu fi-nálnych rafinérskych výrobkov, motorovýchpaliv a technických benzínov alebo ako su-roviny pre pyrolýzu a plynnej fázy vo for-mě paliva.The aforementioned disadvantages of the present state of the art are eliminated by the treatment of waste gases from gasoline production according to the invention, the principle of which is that the waste gases are cooled to 5 to 30 ° C, preferably 15 ° C, with for the condensation of Cs, Ce hydrocarbons, which are fed directly to final-product products, motorized fuels, technical gasoline or used as a raw material for pyrolysis. It is a further object of the invention that the condensed gases are heated to a temperature of 50 ° C to 100 ° C, preferably 70 ° C, in order to achieve complete gasification of the C 8 hydrocarbons, the exhaust gases being burned in the gas burners after the pressure reduction to 2 to 10 kPa and in the case of an increase in the pressure in the degassing system above 30 to 60 kPa, they are combusted in the inert gas burner and refinery heating gas is fed to the gas burner in the case of a pressure reduction in the degassing system below 15 to 30 kPa, while The degassing system below 10-15 kPa is supplied to the gas burners by natural gas as a stable source of gaseous fuel. An advantage of the process of treating waste gases from gasoline production according to the invention is the ability to process even those waste gases which contain heavier components, especially hydrocarbons Cs, Ce and liquid hydrocarbon condensate as a component of refinery refinery products, motor fuels and technical gasoline or as a suction layer for pyrolysis. and a gaseous phase in the form of a fuel.

Na priloženom obrázku je znázorněné za-riadenie k vykonávaniu spósobu spracovaniaodpadových plynov z výroby benzínov po-(Jl’a vynálezu. Technologické zariadenia re-destilácie reformátu a ťažkého benzínu 1, komplexu na reformovanie benzínov 2 ahydrogenačnej rafinácie paliv 3 sú cez re-gulačně ventily nastavené v rozsahu 50 až100 kPa 4, 5 a 6 spojené s kondenzátorom10, v ktorom nastáva výměna tepla medziodpadovými plynmi o teplote až 50 °C achladiacim médiom, obvykle vodou o teplo-te do 20 °C, pri cirkulačnom chladení do 28stupňov Celsia, dochádza ku kondenzácii u-hlovodíkov Cs, C6 a vyšších. Kvapalná fázastéká do odlučovača 11, odkial sa kvapalinaodčerpává čerpadlom 12 do finálnych rafi-nérskych produktov, motorových paliv ale-bo technických benzínov 13. Do motorovýchpaliv, automobíových benzínov, sa s výho-dou přidává táto kvapalná fáza pre vysokéoktánové číslo. Pri nedostatku kvapalnýchnástrekov pre pyrolýzu sa móže kvapalnýkondenzát z odlučovača 11 použiť ako suro-vina pre výrobu etylénu a propylénu pyro-lýzou 14. Odlučovač 11 je spojený potrubímso splyňovačom 18, v ktorom dochádza kvýměně tepla medzi odpadovými plynmi oteplote 15 až 25 °C a ohrevným médiom, ob-vykle nízkotlakovou parou o teplote cca150 °C alebo parným kondenzátom o teploteaspoň 80 °C 19. V splyňovači 18 nastáva do-konalé splynenie uhfovodíkov Cs, Cs, ktorésa nedokonale odlúčili v odlučovači 11, při-padne vykondenzovali v potrubí medzi od-lučovačom 11 a splyňovačom 18 účinkomzníženej teploty, napr. v zimných mesiacoch.Odlučovač 11 je potrubím spojený s pofnýmhorákom 17 cez regulačný ventil 15 riade-ný tlakovým regulátorom 16 nastaveným na30 až 60 kPa. V případe nedostatku odpado-vých plynov zo spracovania benzínov a zní-ženia tlaku za splyňovačom 18 sú do rozvo-du vykurovacieho plynu cez regulačný ven-til 21 riadený tlakovým regulátorom 22 na-staveným na max. 50 % hodnoty tlakovéhoregulátora 16, privádzané rafinérske vyku-rovacie plyny z rozvodu 20. V případe ne-dostatku týchto plynov v rozvode 20 a zní-ženia tlaku v tomto systéme, je do rozvoduvykurovacieho plynu cez regulačný ventil24 riadený tlakovým regulátorom 25 nasta-veným na nižšiu hodnotu ako tlakový regu-látor 22 o 20 až 30 %, privádzaný zemnýplyn 23 ako stabilný zdroj plynného paliva.Požadovaný výkon technologickej pece 26,v ktorej sa ohrieva technologické médium27, je riadený teplotným regulátorom 28riadiacim regulačně ventily 29 a podružné 31, t. j. přívod kvapalného paliva 30, resp.přívod zmesi plynov na kúrenie. Požadova-ný tlak na plynových horákoch, s výhodou5 kPa, je udržiavaný tlakovým regulátorom 32.Referring now to the accompanying drawing, there is shown a device for performing a process for treating waste gas from gasoline production (Ref. No. 1). The technological equipment for re-distillation of reformate and naphtha 1, gasoline reforming complex 2 and hydrogenation refining 3 are via regulating valves. set in the range 50 to 100 kPa 4, 5 and 6 connected to a condenser 10 in which heat exchange between the intermediate waste gases up to 50 ° C occurs and the cooling medium, usually water to a temperature of 20 ° C, with circulating cooling to 28 degrees Celsius occurs To condense the hydrocarbons Cs, C6 and higher, liquid phase flows into the separator 11, where it is pumped by the pump 12 to the final refinery products, motor fuels or technical gasoline 13. Preferably, the fuel is added to the fuel. this liquid phase for the high octane number, in the absence of liquid powders for pyrrole The liquid condensate from the separator 11 can be used as a raw material for the production of ethylene and propylene by pyrolysis 14. The separator 11 is connected by a conduit to a gasifier 18 in which heat exchange occurs between the waste gases of temperature 15 to 25 ° C and the heating medium. with low-pressure steam of about 150 ° C or steam condensate at a temperature of at least 80 ° C 19. The gasification of the Cs, Cs hydrocarbons, which have been imperfectly separated in the separator 11, occurs in the gasifier 18, possibly condensed in the line between the separator 11 and The separator 11 is connected via piping to the burner 17 via a control valve 15 controlled by a pressure regulator 16 set to 30 to 60 kPa. In the event of a shortage of gasoline waste gases and a reduction of the pressure downstream of the gasifier 18, the pressure regulator 22 set to a maximum of 50% of the pressure regulator 16 supplied by the refinery is controlled by the control valve 21 to develop the fuel gas. The diverting gases from the manifold 20. In the absence of these gases in the conduit 20 and the pressure reduction in the system, it is controlled by a pressure regulator 25 set to a lower value than the pressure regulator 22 o by the regulating valve 24 through the regulating valve 24. 20 to 30%, the supplied natural gas 23 as a stable source of gaseous fuel. The required output of the technological furnace 26, in which the process medium 27 is heated, is controlled by a temperature regulator 28 controlling the control valves 29 and a secondary 31, ie a liquid fuel supply 30 or a gas mixture supply. for heating. The required pressure on the gas burners, preferably 5 kPa, is maintained by the pressure regulator 32.

Sposobom na spracovanie odpadovýchplynov z výroby benzínov podlá vynálezusa postupovalo pri spracovaní odpadovýchplynov v jednotke na redestiláciu reformá-tu s kapacitou 395 000 t/r, pričom v odlučo-vači 11 sa zachytilo cca 35 % hmoty odpa-dových plynov, t. j. 1 300 t/r, ktoré sa pou-The process for the treatment of waste gases from gasoline production according to the invention proceeded in the treatment of waste gases in the reformer re-distillation unit with a capacity of 395,000 t / y, while about 35% of the waste gas mass, i.e. 1,300 t / a, was collected in the separator 11. r, which

Claims

23 25 lived as a component for automotive gasoline as a high octane component. The remaining amount of waste gases, 2300 t / a, was burned in a technological furnace on combined oil-gas burners at a pressure of about 5 kPa. For the stabilization burners, the refinery heating gas was for the first time reducing, ie at a pressure of about 20 kPa. The pressure regulator 16 was set at 50 kPa and the pressure regulator 22 at 20 kPa, due to the steady pressure in the refinery heating gas manifold. The gas needed to stabilize the pressure was to use the ground gas from line 23. In Technology 26, the residual products of the column were heated for the redistillation of the reformate, and the capillary was recirculated. For the condensation of liquid hydrocarbons in the condenser 10, a flow rate of 800,000 m 3 / r, t was used. j. 100 m3. h_1. OBJECT

1. A process for treating waste gas from gasoline production, from redistilling a reformed naphtha reformate, from a complex of non-gasoline reformers, and from a hydrogenation refining plant which passes through the control valves to a degassing system by increasing the pressure in such facilities in that the waste gases are cooled to a temperature of 5 ° C to 30 ° C, preferably 15 ° C, with the condensation of C 8 and higher hydrocarbons, which are fed directly to the final refinery products, motor fuels, technical benzines or used as prepyrolysis raw material, non-condensed gases are heated to a temperature of 50 to 100 ° C, preferably 70 degrees Celsius, where after the pressure reduction to 2 to 10 kPa the waste gases are burned in the gas burners and in the case of a pressure increase in the degassing system above 30 to 60kPa there are surpluses gas burned on the field burner.

2. A waste processing method according to claim 1, wherein the refinery heating gas is fed to the gas INVENTION gas burners while reducing the pressure in the degassing system below 15 to 30 kPa, while further reducing the pressure in the degassing system to below 10 to 30 kPa. 15 kPa is supplied by natural gas gas burners as a stable source of gaseous fuel.

3. A waste gas treatment apparatus according to clauses 1 and 2, coupled to process equipment for the reformation of reformate and heavy benzine, to plant for reforming benzene and to a plant for hydrotreating fuels; that the devices are connected, via the control valves (4), (5) and (6), to a capacitor (10) connected to a liquid phase separator (11) which is connected to the degassing system via a control valve (15) a burner burner (17), on the one hand, through a gasifier (18) with a heating furnace manifold of the process furnace (26), wherein the fuel gas distribution is connected to the refinery gas distribution (20), the natural gas distribution (23) and the regulating a valve (31) with furnace burners (26). 1 sheet of drawings