HRP980400A2 - Apparatus for the continuous distillative separation of crude oil - Google Patents
Apparatus for the continuous distillative separation of crude oilInfo
- Publication number
- HRP980400A2 HRP980400A2 HRA1229/97A HRP980400A HRP980400A2 HR P980400 A2 HRP980400 A2 HR P980400A2 HR P980400 A HRP980400 A HR P980400A HR P980400 A2 HRP980400 A2 HR P980400A2
- Authority
- HR
- Croatia
- Prior art keywords
- heat exchanger
- crude oil
- furnace
- waste gas
- pipeline
- Prior art date
Links
- 239000010779 crude oil Substances 0.000 title claims description 48
- 238000007700 distillative separation Methods 0.000 title 1
- 239000007789 gas Substances 0.000 claims description 34
- 239000002912 waste gas Substances 0.000 claims description 27
- 238000004821 distillation Methods 0.000 claims description 20
- 238000002485 combustion reaction Methods 0.000 claims description 13
- 239000000446 fuel Substances 0.000 claims description 9
- 239000003921 oil Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 239000000523 sample Substances 0.000 claims description 6
- 238000001944 continuous distillation Methods 0.000 claims description 5
- 238000001704 evaporation Methods 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 description 18
- 239000002918 waste heat Substances 0.000 description 11
- 239000000047 product Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- MHCVCKDNQYMGEX-UHFFFAOYSA-N 1,1'-biphenyl;phenoxybenzene Chemical group C1=CC=CC=C1C1=CC=CC=C1.C=1C=CC=CC=1OC1=CC=CC=C1 MHCVCKDNQYMGEX-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
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
- C10G7/00—Distillation of hydrocarbon oils
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (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)
Description
Predmet izuma je uređaj za kontinuirano destilacijsko rastavljanje sirove nafte s kolonom za destilaciju. The subject of the invention is a device for continuous distillation separation of crude oil with a distillation column.
Pri destilacijskom rastavljanju sirove nafte posebno visok značaj ima njeno jednakomjerno zagrijavanje. S jedne strane treba paziti na to da se sirovu naftu grije jednakomjerno, pri čemu istovremeno vrijeme zadržavanja u uređaju za grijanje, u kojem se nafta zagrijava primjerice od 20 do 360ºC do 400ºC , posebno treba biti vrlo kratko da se spriječi razgradnju sirove nafte. Tako su cijevne peći, primjerice, opremljene s pokretnim ložištem ako se upotrebljava kruto gorivo, ili s mlaznicama za ulje ili plin. Sistem cijevne zavojnice, kroz koji se pumpa sirovu naftu, grije se s vrućim plinovima. During the distillation separation of crude oil, its even heating is particularly important. On the one hand, care should be taken to ensure that the crude oil is heated evenly, while at the same time the residence time in the heating device, in which the oil is heated for example from 20 to 360ºC to 400ºC, should be especially short to prevent the decomposition of the crude oil. Thus, tubular furnaces are, for example, equipped with a movable firebox if solid fuel is used, or with nozzles for oil or gas. The tube coil system, through which the crude oil is pumped, is heated with hot gases.
Da se provede ekonomičnije grijanje nafte, upotrebljavaju se takozvane radijacijske peći, u kojima se cjevovod za sirovu naftu stavlja u komore odvojene od plamenika, tako da se primjerice sirova nafta može polako grijati u donjem temperaturnom području, a brzo u gornjem temperaturnom području, da se ograniči stvaranje koksa. In order to heat oil more economically, so-called radiation furnaces are used, in which the pipeline for crude oil is placed in chambers separated from the burner, so that, for example, crude oil can be heated slowly in the lower temperature range, and quickly in the upper temperature range, to limit the formation of coke.
Pored cijevnih peći poznate su također i stojeće cilindrične peći, u kojima je predviđena okomita cilindrična komora za sagorijevanje, koja je okružena s kružno raspoređenim stojećim cijevima. Na dnu cilindrične peći raspoređene su mlaznice za sagorijevanje kod plinskog grijanja, dok je u gornjem području predviđen radijacijski stožac, koji skrbi za jednakomjerni prijenos topline od plinova na snop cijevi. In addition to tube furnaces, standing cylindrical furnaces are also known, in which a vertical cylindrical combustion chamber is provided, which is surrounded by circularly arranged standing pipes. At the bottom of the cylindrical furnace, there are combustion nozzles for gas heating, while a radiation cone is provided in the upper area, which ensures the uniform transfer of heat from the gases to the bundle of pipes.
Pored što je moguće jednakomjernijeg prijenosa topline, od posebnog je značaja njihovo efikasno iskorištenje. Pri izradi energetske bilance u pogonu za preradu nafte, treba računati s energetskim utroškom od pribl. 5% sirove naftu koju se prerađuje za utrošenu toplinsku energiju. Prema tome, ponovnom dobivanju i upotrebi otpadne topline posvećuje se posebno veliku pažnju. Tako se otpadnu toplinu od pojedinačnih frakcija koristi za predgrijavanje zraka, primjerice za peći sa sagorijevanjem ili također za predgrijavanje drugih frakcija. Otpadnu toplinu upotrebljava se također i za proizvodnju pare za vlastite potrebe u rafineriji, kao također i za vanjsko grijanje. In addition to the most even possible heat transfer, their efficient use is of particular importance. When creating an energy balance in an oil processing plant, one should calculate the energy consumption of approx. 5% of crude oil that is processed for used thermal energy. Therefore, special attention is paid to the recovery and use of waste heat. Thus, waste heat from individual fractions is used for air preheating, for example for combustion furnaces or also for preheating other fractions. Waste heat is also used to produce steam for own needs in the refinery, as well as for external heating.
Da bi se ograničio utrošak sirove nafte ili njenih proizvoda za dovod topline unutar rafinerije nafte, dosad su već bili predloženi najrazličitiji izvori topline (13. World Petrol Congress Buenos Aires 1991, Proseedings V3, 297 do 301). Tako je općenito predloženo iskorištavanje topline plinom hlađenog nuklearnog reaktora visoke temperature, što nije bio ostvareno, zatim iskorištavanje sunčeve energiju, koja uzrokuje previsoke investicijske troškove, a također i otpadnu toplinu plinskih turbina, koje se zbog radova održavanja moraju isključivati u kratkim razmacima. In order to limit the consumption of crude oil or its products for the supply of heat inside the oil refinery, a wide variety of heat sources have already been proposed (13th World Petrol Congress Buenos Aires 1991, Proceedings V3, 297 to 301). Thus, it was generally proposed to use the heat of a gas-cooled high-temperature nuclear reactor, which was not realized, then to use solar energy, which causes too high investment costs, and also the waste heat of gas turbines, which must be turned off at short intervals due to maintenance work.
Cilj predloženog izuma stvoriti uređaj za kontinuiranu destilaciju sirove nafte, pri čemu se sirovu naftu može zagrijati posebno ekonomično, kontinuirano i jednakomjerno do temperature između 350ºC i 400ºC također kod različitih potreba topline, pri čemu se istovremeno dobije električnu energiju, a otpadnu toplinu se može kvalitetno iskoristiti. The aim of the proposed invention is to create a device for the continuous distillation of crude oil, whereby the crude oil can be heated particularly economically, continuously and evenly to a temperature between 350ºC and 400ºC also with different heat needs, while at the same time electricity is obtained, and the waste heat can be qualitatively use.
Upotrebi plinskih turbina kod destilacijskog rastavljanje sirove nafte suprotstavlja se to da je za plinske turbine potrebno u kratkoročnim višemjesečnim razmacima održavanje, dok nasuprot tome, da se osigura potrebu ekonomičnost, uređaji za kontinuirano destilacijsko rastavljanje sirove nafte moraju biti tijekom godine neprekidno u pogonu. Da se dobije željeni sastav proizvoda, čak i samo ograničene promjene uvjetuju skupe postupke podešavanja. Također, pri stavljanju nove sirove nafte u kolonu za destilaciju postupak destilacije u koloni mora se ponovno podesiti, pri čemu se mora točno unaprijed zadati i regulirati temperaturu ulazne sirove nafte, količinu povratnog toka u kolonu za destilaciju i sa se osigura potrebu ekonomičnost, uređaji za kontinuirano destilacijsko rastavljanje sirove nafte moraju biti tijekom godine neprekidno u pogonu. Da se dobije željeni sastav proizvoda, čak i samo ograničene promjene uvjetuju skupe postupke podešavanja. Također, pri stavljanju nove sirove nafte u kolonu za destilaciju postupak destilacije povezana posredno, odnosno neposredno sa zonom isparavanja destilacijske kolone s prihvatnim dnom, naročito zvonastim dnom, sa striperima, koji su povezani barem s dva različita prihvatna dna i s jednim generatorom vodene pare i/ili pregrijačem i s jednim gornjim hladilom, sastoji se uglavnom u tome da je dodatno predviđena jedna plinska turbina, koja je povezana sa strujnim generatorom i s izmjenjivačem topline otpadnih plinova za sirovu naftu, preko kojeg se sirova nafta može grijati izravno i/ili posredno. The use of gas turbines in the distillation separation of crude oil is opposed by the fact that gas turbines require maintenance in short-term intervals of several months, while on the other hand, to ensure the need for economy, devices for continuous distillation separation of crude oil must be continuously in operation throughout the year. To obtain the desired product composition, even only limited changes require expensive adjustment procedures. Also, when putting new crude oil into the distillation column, the distillation process in the column must be re-adjusted, whereby the temperature of the incoming crude oil, the amount of return flow into the distillation column must be accurately set and regulated in advance, and with the need to ensure economy, devices for continuous distillation separation of crude oil must be continuously in operation during the year. To obtain the desired product composition, even only limited changes require expensive adjustment procedures. Also, when putting new crude oil into the distillation column, the distillation process is connected indirectly, i.e. directly to the evaporation zone of the distillation column with a receiving bottom, especially a bell bottom, with stripers, which are connected to at least two different receiving bottoms and one water vapor generator and/ or a superheater and with one upper cooler, consists mainly in the fact that one gas turbine is additionally provided, which is connected to the current generator and to the waste gas heat exchanger for crude oil, through which the crude oil can be heated directly and/or indirectly.
Time da je dodatno za plinsku turbinu predviđena peć, destilacijsko rastavljanje sirove nafte može se i dalje provoditi kod radova održavanja na plinskoj turbini, pri čemu se upravljanjem snage grijanja peći pokrivaju različite potrebe za toplinom i time se može osigurati jednakomjernu snagu plinske turbine. Since a furnace is additionally provided for the gas turbine, the distillation separation of crude oil can still be carried out during maintenance work on the gas turbine, whereby different heat needs are covered by controlling the heating power of the furnace and thus the uniform power of the gas turbine can be ensured.
Kod iskorištavanja samog po sebi visokog potencijala otpadne topline plinske turbine, mora se posebno paziti na to da je otpor strujanju otpadnih plinova u izmjenjivaču topline vrlo malen, da se time ne smanjuje električnu snagu plinske turbine, čime se i kod velikog presjeka strujanja dobiju relativno velike površine, uzduž kojih se provodi izmjena topline. Pored tih općih uvjeta, koji uzrokuju skupu izmjenu topline, dodatno je potrebno da se kapacitet peći drži tako velikim, da ona bez dodatnog grijanja s plinskom turbinom može zagrijati sirovu naftu na željenu temperaturu. Umjesto jedne peći, da se primjerice kod male snage grijanja dobije bolji stupanj iskorištenja, predviđene su dvije ili više peći. Te peći mogu imati jedinstveno grijanje, primjerice plinsko grijanje. Međutim, može se zamisliti također i drugačije gorivo kao ulje, kruto gorivo, koje se također može spaliti u vrtložnoj slojevitoj peći. When exploiting the inherently high waste heat potential of the gas turbine, special attention must be paid to the fact that the resistance to the flow of waste gases in the heat exchanger is very small, so that the electric power of the gas turbine is not thereby reduced, which results in relatively large flow cross-sections surfaces, along which heat exchange is carried out. In addition to these general conditions, which cause expensive heat exchange, it is additionally necessary that the capacity of the furnace is kept so large that it can heat the crude oil to the desired temperature without additional heating with a gas turbine. Instead of one furnace, in order to obtain a better level of utilization, for example, with low heating power, two or more furnaces are provided. These stoves can have unique heating, for example gas heating. However, a different fuel than oil, a solid fuel, can also be imagined, which can also be burned in a fluidized bed furnace.
Ako je izmjenjivač topline otpadnih plinova povezan cjevovodom za medij koji prenosi toplinu s daljnjim izmjenjivačem topline za sirovu naftu, tada se može poslužiti za posebno ekonomično grijanju sirove nafte, jer se vršne temperature, kao što su one u dimnim plinovima, ni u kojem slučaju se ne predaju dalje sirovoj nafti. Nadalje, time se može postići da se otpadna toplina plinske turbine ne upotrebljava samo za grijanje sirove nafte već se također može upotrijebiti i za daljnje potrebe. If the waste gas heat exchanger is connected by a heat transfer medium pipeline to a further crude oil heat exchanger, then it can be used for particularly economical heating of crude oil, because peak temperatures, such as those in the flue gases, in no case they do not pass on to crude oil. Furthermore, it can be achieved that the waste heat of the gas turbine is not only used for heating crude oil, but can also be used for further needs.
Ako je izmjenjivač topline otpadnih plinova i/ili daljnji izmjenjivač topline povezan serijski s peći (pećima), tada se može osigurati jedinstvenu temperaturu u koloni za destilaciju ulazne sirove nafte bez dodatnih uređaja, kao što su primjerice mješalica u kojima se miješa sirovu naftu iz izmjenjivača topline, odnosno peći. Time je data ušteda na troškovima za uređaje uz istovremeno povišenje sigurnosti procesa. If the waste gas heat exchanger and/or a further heat exchanger is connected in series with the furnace(s), then a uniform temperature can be ensured in the column for the distillation of the incoming crude oil without additional devices, such as mixers in which the crude oil from the exchanger is mixed heat, or stove. This provides savings on device costs while simultaneously increasing process safety.
Ako je plinska turbina, u odnosu na otpadne plinove, priključena iza dodatnog ložišta sa cjevovodom za gorivo u otpadnim plinovima, tada se s jedne strane može postići dodatno grijanje otpadnih plinova, a s druge strane može se spaliti udio kisika koji je još prisutan u otpadnim plinovima, čime se može postići veća sigurnost kod rukovanja s otpadnim plinovima, primjerice kod izravnog grijanja nafte. If the gas turbine, in relation to the waste gases, is connected behind an additional combustion chamber with a pipeline for fuel in the waste gases, then on the one hand additional heating of the waste gases can be achieved, and on the other hand the portion of oxygen still present in the waste gases can be burned , by which greater safety can be achieved when handling waste gases, for example when directly heating oil.
Ako je u smjeru strujanja sirove nafte izmjenjivač topline otpadnih plinova i/ili daljnji izmjenjivač topline raspoređen ispred barem jedne peći, tada se može provesti posebno ekonomično grijanje sirove nafte, jer se u peći može podignuti na željeni visoki temperaturni potencijal, koja što se tiče brzine strujanja medija za izmjenu topline ne podliježe ograničenjima, kao izmjenjivač topline plinske turbine. Nadalje, pretvaranje sirove nafte u koks može se spriječiti odnosno držati posebno niskim. If, in the direction of the flow of crude oil, a waste gas heat exchanger and/or a further heat exchanger is arranged in front of at least one furnace, then a particularly economical heating of the crude oil can be carried out, because it can be raised to the desired high temperature potential in the furnace, which in terms of speed the flow of the heat exchange medium is not subject to restrictions, like a gas turbine heat exchanger. Furthermore, the conversion of crude oil into coke can be prevented or kept particularly low.
Ako je barem jedan grijač vode i/ili generator vodene pare i/ili pregrijač povezan cjevovodom s ulazom i izlazom medija za prijenos topline izmjenjivača topline otpadnih plinova, tada se otpadnu toplinu iz plinske turbine može upotrijebiti za proizvodnju tople vode ili vodene pare, koja je potrebna primjerice za stripere. If at least one water heater and/or steam generator and/or superheater is connected by piping to the inlet and outlet of the heat transfer medium of the waste gas heat exchanger, then the waste heat from the gas turbine can be used to produce hot water or steam, which is needed, for example, for stripers.
Ako je ispred peći predviđena temperaturna mjerna sonda za sirovu naftu, npr. u izmjenjivaču topline otpadnih plinova i/ili u daljnjem izmjenjivaču topline, preko koje se upravlja, odnosno regulira dovod goriva u peć i/ili dodatno ložište, tada se na posebno jednostavan način može snagu plinske turbine držati pri željenoj veličini, jer se ne moraju se uračunavati različite potrebe topline različitih sirovih nafti, različite viskoznosti i time otpori strujanju i različite protočne količine u izmjenjivaču topline otpadnog plina, odnosno daljnjem izmjenjivaču topline plinske turbine, već se taj dodatni dovod topline u peć, odnosno dodatno ložište može jednostavno upravljati, odnosno regulirati. If a temperature measuring probe for crude oil is provided in front of the furnace, for example in the waste gas heat exchanger and/or in a further heat exchanger, through which the fuel supply to the furnace and/or additional combustion chamber is controlled or regulated, then in a particularly simple way can keep the power of the gas turbine at the desired level, because the different heat needs of different crude oils, different viscosities and thus flow resistances and different flow rates in the waste gas heat exchanger, i.e. the further heat exchanger of the gas turbine, do not have to be taken into account, but this additional supply of heat to the furnace, i.e. the additional firebox can be easily managed or regulated.
Ako je predviđena temperaturna mjerna sonda za sirovu naftu, koja napušta peć, preko koje se upravlja, odnosno regulira dovod goriva u peć i/ili dodatno ložište, tada se regulaciju, odnosno vođenje snage grijanja peći i/ili dodatnog ložišta može dobiti izravno preko izlazne temperature sirove nafte. If a temperature measuring probe is provided for the crude oil, which leaves the furnace, through which the fuel supply to the furnace and/or additional combustion chamber is controlled, i.e. regulated, then regulation, i.e. control of the heating power of the furnace and/or additional combustion chamber can be obtained directly via the output crude oil temperature.
U nastavku se izum pobliže objašnjava pomoću crteža, od kojih In the following, the invention is explained in more detail with the help of drawings, of which
slika 1 prikazuje shemu za grijanje sirove nafte i Figure 1 shows a scheme for heating crude oil and
slika 2 shematski prikazuje kolonu za destilaciju s dodatnim agregatima. Figure 2 schematically shows a distillation column with additional aggregates.
Plinska turbina GT, prikazana na slici 1, s brojem okretaja 3000 odnosno 3600 okr./min, mehanički je povezana sa strujnim generatorom G. Plinska turbina ima utrošak od 7500 m3/h zemnog plina. Ona je aeroderiativna turbina, npr. LM 2500 tvrtke General Electric, ili DLE 2500 tvrtke General Electric, s manjom početnom emisijom oksida. Generator daje 30.000 kW. Plinovi, koji izlaze iz plinske turbine s temperaturom od 510ºC , ulaze u dodatno ložište NB, u kojem izgara preostali kisika s dodatno uvedenim zemnim plinom (strelica a). Plinovi koji izlaze iz dodatnog ložišta imaju temperaturu od 700ºC. U izmjenjivaču topline otpadnih plinova W1 otpadni plinovi predaju svoju toplinu mediju koji prenosi toplinu, i to Diphylu (do 350ºC ). Medij koji prenosi toplinu u cjevovod w povezuje izmjenjivač topline otpadnih plinova W1 s daljnjim izmjenjivačem topline W2. The gas turbine GT, shown in Figure 1, with a speed of 3000 and 3600 rpm, is mechanically connected to the current generator G. The gas turbine has a consumption of 7500 m3/h of natural gas. It is an aeroderivative turbine, eg LM 2500 from General Electric, or DLE 2500 from General Electric, with lower initial oxide emissions. The generator produces 30,000 kW. The gases leaving the gas turbine with a temperature of 510ºC enter the additional combustion chamber NB, where the remaining oxygen is burned with additionally introduced natural gas (arrow a). The gases coming out of the additional combustion chamber have a temperature of 700ºC. In the waste gas heat exchanger W1, the waste gases transfer their heat to a medium that transfers heat, namely Diphyl (up to 350ºC). The heat transfer medium in the pipeline w connects the waste gas heat exchanger W1 with a further heat exchanger W2.
U daljnji izmjenjivač topline W2 uvodi se kroz cjevovod L1 sirovu naftu temperature 140ºC i dospjeva ona preko cjevovoda L2 s 250ºC dolazi u plinske peći 1, 2, u kojima se još dodatno zagrije na 370ºC. Daljnji izmjenjivač topline W2 i peći 1, 2 su povezani serijski. Cjevovod w može također voditi još prema generatoru pare D, u kojem se stvara para za postupak skidanja. Za iskorištavanje otpadne topline, otpadni plinovi iz izmjenjivača topline W1 odvode se u izmjenjivač topline W3, u kojem se grije voda za vanjsko grijanje. Crude oil at a temperature of 140ºC is introduced into the further heat exchanger W2 through the pipeline L1, and it arrives via the pipeline L2 at 250ºC and enters the gas furnaces 1, 2, where it is further heated to 370ºC. Further heat exchanger W2 and furnaces 1, 2 are connected in series. The pipeline w can also lead further to the steam generator D, in which steam is generated for the stripping process. To utilize the waste heat, the waste gases from the heat exchanger W1 are led to the heat exchanger W3, in which the water for external heating is heated.
Otpadni plinovi iz plinske peći 1, 2 hlade se preko izmjenjivača topline W4 i toplina odlazi za stvaranje procesne pare koju se upotrebljava unutar rafinerije. Temperatura otpadnih plinova drži se iznad 100ºC , tako da u kaminu ne dolazi do nikakve kondenzacije. Preko cjevovoda L3 dovodi se sirovu naftu zagrijanu na 370ºC u kolonu za destilaciju. The waste gases from the gas furnace 1, 2 are cooled via the heat exchanger W4 and the heat goes to create process steam that is used inside the refinery. The temperature of waste gases is kept above 100ºC, so that no condensation occurs in the fireplace. Through pipeline L3, crude oil heated to 370ºC is fed into the distillation column.
U cjevovodu za sirovu naftu L2, koji povezuje daljnji izmjenjivač topline W2 s peći 1, 2, nalazi se temperaturna mjerna sonda T1, koja regulira protok ventila V1 za plin u peći 1, 2, ali također i dovod goriva, strelica a, za dodatno ložište NB. U izlaznoj cijevi L3 nalazi se daljnja temperaturna mjerna sonda T2, koja sa svoje strane pazi na regulaciju i upravljanje protočne količine ventila V2, čime se također može regulirati i upravljati količinu plina koja se dovodi u peć, ali također i dovod goriva za dodatno ložište i time snagu grijanja. Postupak destilacije opisat će se pobliže u nastavku pomoću slike 2. In the crude oil pipeline L2, which connects the further heat exchanger W2 to the furnace 1, 2, there is a temperature measuring probe T1, which regulates the flow of the gas valve V1 in the furnace 1, 2, but also the fuel supply, arrow a, for additional fire pit NB. In the outlet pipe L3 there is a further temperature measuring probe T2, which in turn takes care of the regulation and management of the flow rate of the valve V2, which can also regulate and manage the amount of gas fed to the furnace, but also the supply of fuel for the additional combustion chamber and thus the heating power. The distillation process will be described in more detail below using Figure 2.
Sirova nafta dolazi iz peći 1 i 2 kroz cjevovod L3 u kolonu za skidanje 3, u koju se prema strelici X1 dovodi paru. U kolonu za skidanje (3) dolazi nadalje (strelica L) dio proizvoda s dna iz sabirnice destilacijske kolone 4. Sirova nafta, koja se uvodi kroz cjevovod L3, zagrije se otpadnom toplinom iz plinske turbine i pomoću peći 1, 2 na 370ºC . U koloni za skidanje 3 sirova nafta se rasterećuje s 5 bara na 3 bara i zatim se cjevovodom X2 odvodi u zonu isparavanja kolone za destilaciju 4. Pri tome dolazi do daljnjeg rasterećenja na 1,5 bar. U koloni 4 za destilaciju nalazi se 45 zvonolikih tanjura. U stripere 5, 6 i 7 uvodi se s jedne strane proizvod izvučen iz kolone za destilaciju, koji izlaže se pari preko cjevovoda D1, D2, D3 i time se istjeruju lakše hlapljivi sastojci. Dobiveni materijal izvlači se u sabirnici stripera, dok se glavni proizvod ponovno dovodi u kolonu. Para, koja se upotrebljava u striperima, dobiva se s otpadnom toplinom plinske turbine u generatoru pare D (slika 1). Krajnji proizvod, izvučen iz stripera, hladi se preko izmjenjivača topline W5, W6 i W7. Kolona za destilaciju 4 ima nadalje gornje hladilo 8. Crude oil comes from furnaces 1 and 2 through pipeline L3 to stripping column 3, into which steam is fed according to arrow X1. In the removal column (3) comes further (arrow L) a part of the product from the bottom of the bus of distillation column 4. Crude oil, which is introduced through the pipeline L3, is heated by waste heat from the gas turbine and by means of furnaces 1, 2 to 370ºC. In the stripping column 3, the crude oil is relieved from 5 bar to 3 bar and then it is taken to the evaporation zone of the distillation column 4 through pipeline X2. In doing so, it is further relieved to 1.5 bar. There are 45 bell-shaped plates in column 4 for distillation. In the strippers 5, 6 and 7, the product extracted from the distillation column is introduced on one side, which is exposed to steam through pipelines D1, D2, D3, and thus more volatile ingredients are expelled. The obtained material is extracted in the stripper bus, while the main product is fed back into the column. The steam, which is used in the strippers, is obtained with the waste heat of the gas turbine in the steam generator D (Figure 1). The final product, extracted from the stripper, is cooled via heat exchangers W5, W6 and W7. The distillation column 4 also has an upper cooler 8.
Claims (8)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT0122997A AT406165B (en) | 1997-07-18 | 1997-07-18 | DEVICE FOR CONTINUOUS DISTILLATIVE SEPARATION OF RAW OIL |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| HRP980400A2 true HRP980400A2 (en) | 1999-10-31 |
| HRP980400B1 HRP980400B1 (en) | 2001-08-31 |
Family
ID=3509403
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| HR980400A HRP980400B1 (en) | 1997-07-18 | 1998-07-16 | Apparatus for the continuous distillative separation of crude oil |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0892030B1 (en) |
| AT (1) | AT406165B (en) |
| BG (1) | BG63400B1 (en) |
| DE (1) | DE59805483D1 (en) |
| ES (1) | ES2181156T3 (en) |
| HR (1) | HRP980400B1 (en) |
| PT (1) | PT892030E (en) |
| SI (1) | SI0892030T1 (en) |
| SK (1) | SK283465B6 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2417984B (en) * | 2004-09-09 | 2009-11-04 | M W Kellogg Ltd | Integrated process plant utilising a fractionating auxilliary treatment system |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3567628A (en) * | 1968-10-25 | 1971-03-02 | Phillips Petroleum Co | Production of high flash point topped crude and high flash point asphalt |
| FR2258443B1 (en) * | 1974-01-17 | 1976-11-26 | Spie Batignolles | |
| US5247907A (en) * | 1992-05-05 | 1993-09-28 | The M. W. Kellogg Company | Process furnace with a split flue convection section |
| JP2554229B2 (en) * | 1992-10-26 | 1996-11-13 | 三菱重工業株式会社 | Combined cycle power generation method |
-
1997
- 1997-07-18 AT AT0122997A patent/AT406165B/en not_active IP Right Cessation
-
1998
- 1998-07-14 DE DE59805483T patent/DE59805483D1/en not_active Expired - Lifetime
- 1998-07-14 SI SI9830296T patent/SI0892030T1/en unknown
- 1998-07-14 ES ES98890204T patent/ES2181156T3/en not_active Expired - Lifetime
- 1998-07-14 PT PT98890204T patent/PT892030E/en unknown
- 1998-07-14 EP EP98890204A patent/EP0892030B1/en not_active Expired - Lifetime
- 1998-07-16 HR HR980400A patent/HRP980400B1/en not_active IP Right Cessation
- 1998-07-16 SK SK973-98A patent/SK283465B6/en not_active IP Right Cessation
- 1998-07-20 BG BG102642A patent/BG63400B1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| EP0892030A2 (en) | 1999-01-20 |
| BG102642A (en) | 1999-02-26 |
| ATA122997A (en) | 1999-07-15 |
| AT406165B (en) | 2000-03-27 |
| DE59805483D1 (en) | 2002-10-17 |
| EP0892030B1 (en) | 2002-09-11 |
| PT892030E (en) | 2003-01-31 |
| SI0892030T1 (en) | 2003-04-30 |
| HRP980400B1 (en) | 2001-08-31 |
| BG63400B1 (en) | 2001-12-29 |
| EP0892030A3 (en) | 1999-07-28 |
| ES2181156T3 (en) | 2003-02-16 |
| SK283465B6 (en) | 2003-08-05 |
| SK97398A3 (en) | 1999-02-11 |
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