SU506302A3 - The method of producing liquefied petroleum gas - Google Patents
The method of producing liquefied petroleum gasInfo
- Publication number
- SU506302A3 SU506302A3 SU1812197A SU1812197A SU506302A3 SU 506302 A3 SU506302 A3 SU 506302A3 SU 1812197 A SU1812197 A SU 1812197A SU 1812197 A SU1812197 A SU 1812197A SU 506302 A3 SU506302 A3 SU 506302A3
- Authority
- SU
- USSR - Soviet Union
- Prior art keywords
- petroleum gas
- liquefied petroleum
- producing liquefied
- bbl
- hydrocracking
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/10—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/28—Propane and butane
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
городные металлы VIII труппы содержатс в количества 0,01-2 isec. %.City metals of Group VIII are contained in an amount of 0.01-2 isec. %
.Процесс гидрокрекинга провод т при 343-510° С. Наиболее оптима.тьной вл етс температура 351-483° С. Давление в зоне реак1ции гидрокрекинга 70,3-175,8 кг/сж, скорость 1подачи углеводородов 0,25-5 единиц объемной часовой скорости жидкости. Концентраци водорода м /баррель. В качестве Катализатора гидрокрекинга используют один ИЛИ несколько металлов IVB и VII групп Периодической системы элементов, например олово, германий, .нанесейных на кремнезем , .содержащий 12-30 вес. % глинозема.The hydrocracking process is carried out at 343-510 ° C. The most optimal temperature is 351-483 ° C. The pressure in the hydrocracking reaction zone is 70.3-175.8 kg / ss, the rate of hydrocarbon delivery is 0.25-5 units volumetric hourly velocity of the fluid. Hydrogen concentration m / bbl. As a hydrocracking catalyst, one OR several metals of the IVB and VII groups of the Periodic Table of the elements are used, for example, tin, germanium, nonscore on silica, containing 12-30 wt. % alumina.
На второй стадии гидрокреки-нга может быть .применен катализатор, в котором металлические ком поненты прап-итывают кристаллические алюмосиликатные молекул рные сита. В качест1ве молекул рного сита могут быть использованы морденит, .молекул рные сита типа X и Y, а также цеолитсодержащий материал, диспергированный в аморфной матрице глинозема, крем.незема или алюмосиликата .In the second hydrocrack stage, a catalyst may be used in which the metallic components pore crystalline aluminosilicate molecular sieves. Mordenite, molecular sieves of types X and Y, as well as zeolite-containing material dispersed in an amorphous alumina matrix, silica gel or aluminosilicate can be used as molecular sieves.
Реакции гидрокрекинга Я|вл ютс в основном экзотермически.ми реакци ми. При прохождении сырь и водорода через слой катал .изатора на1блю1даетс повышение тэмпе-ратуры . Поэтому во избежание очень сильного повышени температуры в зонах гидрокрекинга IB одном или нескольких пунктах этих зон 1подают охлаждающий IHOTOK жидкости или газов.Hydrocracking reactions I | are mainly exothermic reactions. With the passage of raw materials and hydrogen through the bed of the catalyst, an increase in temperature is observed. Therefore, in order to avoid a very high temperature increase in the hydrocracking zones IB, one or several points of these zones 1 supply cooling IHOTOK liquids or gases.
Пример I. Получение сжиженного нефт ного газа из т желого углеводородного сырь с концом кипени 547° С.Example I. Production of liquefied petroleum gas from heavy hydrocarbon feedstock with a boiling point of 547 ° C.
На чертеже .изображена схема установки дл .реализаЦИИ этого процесса.In the drawing. Depicts the setup diagram for the implementation of this process.
ХараКтбристика сырь :Characteristics of raw materials:
Плотность, ,8756 Пнтервал перегонки, °С: Начальна точ:ка кипени 210 1.0%338 30%360 50%377 70%398 90%448 Конечна .ка килени 549 Сера, вес. %0,93 Азот, ч./млн.600Density,, 8756 Distillation interval, ° С: Starting point: boiling point 210 1.0% 338 30% 360 50% 377 70% 398 90% 448 Endpoint, 549 Sulfur, wt. % 0.93 Nitrogen, hours per million 600
сырье подвертают гидроочистке с иопользование.м катализатора, состо щего из глниоземно-кремиеземного носител , содержащего 37 .вес. % кремнезема, 1,8 овес. % ликел , 16 вес. % молибдена. iB зоне реакции поддержевают давление 140 кг1см и температуру в слое катализатора 455° С. Скорость подач.и сырь 4500 баррель, концентраци водорода гоколо 186 м /баррель, объемна часова скорость жидкости 0,70. Потребление водорода ,в системе гидроочистки 1,32% от общего веса сььрь . Данные о выходе и распределении продуктов при гидроочистке приведены в табл. 1. the raw material is hydrotreated using a catalyst consisting of a glyozem-cremiesel carrier containing 37 weight. % silica, 1.8 oats. % liquor, 16 wt. % molybdenum. The iB reaction zone maintains a pressure of 140 kg1 cm and a temperature in the catalyst bed of 455 ° C. The feed rate and raw material are 4500 bbl, the concentration of hydrogen is about 186 m / bbl, the volumetric rate of the liquid is 0.70. The hydrogen consumption in the hydrotreating system is 1.32% of the total weight of the fuel. Data on the yield and distribution of products during hydrotreatment are given in table. one.
т а б л II ц а 1t a b l ii c a 1
ВыходOutput
КомпонентComponent
, л. I барое.1}/ день, l I bar.1} / day
Из табл. 1 следует, что, хот основнымиFrom tab. 1 it follows that although the main
реакци ми вл ютс десульфурирование и денитраци , значительна часть (Продуктов крекируетс в низкокип щие углеводороды. В сжиженный (Нефт ной -газ следует ввести 111 баррель/день колцентрата пропана-бутана;The reactions are desulfurization and denitration, a significant part (Products are cracked into low-boiling hydrocarbons. In a liquefied (Oil-gas, 111 barrels / day of propane-butane concentrate should be introduced;
фракцию С7-200° С в колличестве 634 баррель/день следует на1пра1вить на вторую стадию гидрокрекин1га.The C7-200 ° C fraction in the amount of 634 bbl / day should be put on the second stage of hydrocracking.
4,03.5 баррель/день углеводородов, кип щих выше 200° С, служит сырьем дл д.вухстадийного 1процесса, подаваемым по линии 1. Отношение потока углеводородов, кип щих выше 200° С, к рециркулируемой жидкой фазе первой стадии процесса составл ет 1,6. Указанное выше сырье в линии 1 смешивают с4.03.5 bbl / day of hydrocarbons boiling above 200 ° C is used as feedstock for the two-stage 1 process fed through line 1. The ratio of hydrocarbons boiling above 200 ° C to the recycled liquid phase of the first stage of the process is 1, 6 The above raw materials in line 1 are mixed with
2,400 баррель/день рециркулИруемой жидкой фазой первой стадии, подаваемой по л.инии 2, и с i283 м /баррель рециркулируемого водорода , поступающего ino линии 3.2,400 bbl / day of recirculated liquid phase of the first stage supplied by line 2 and i283 m / bbl of recycled hydrogen coming ino line 3.
Полученна смесь .направл етс по линии 1The resulting mixture is directed along line 1
в реактор 4 гидрокрекинга, где поддерживают давление около 141 кг/см .и температуру в слое катализатора около 400° С. Часова Объем.на скорость жидкости из расчета 4,035 баррель/день свежего сырь составл етto the hydrocracking reactor 4, where the pressure is maintained at about 141 kg / cm and the temperature in the catalyst bed is about 400 ° C. The clock volume per fluid rate is 4,035 bbl / day of fresh raw material
0,81. Эфлюент падают по линии 5 в гор чий Сгпаратор 6 при .давлении 146 кг/см и температуре 204° С. В та|бл. 2 приведены .данные D выходе и составе Продуктов, поступающих из реактора 4.0.81. The effluent falls along line 5 to the hot Cgparator 6 at a pressure of 146 kg / cm and a temperature of 204 ° C. In ta | bl. 2 shows the D output data and the composition of the Products coming from the reactor 4.
Таблица 2table 2
ВыходOutput
Основна «арообразна фаза, поступающа .из гор чего сепаратора 6 по линии 7, соедин етс с напрореатировавщей нафтой вThe main ar-like phase, coming from the hot separator 6 through line 7, is connected to naphtha with naphtha in
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US16158671A | 1971-07-12 | 1971-07-12 |
Publications (1)
Publication Number | Publication Date |
---|---|
SU506302A3 true SU506302A3 (en) | 1976-03-05 |
Family
ID=22581812
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
SU1812197A SU506302A3 (en) | 1971-07-12 | 1972-07-12 | The method of producing liquefied petroleum gas |
Country Status (16)
Country | Link |
---|---|
US (1) | US3718575A (en) |
JP (1) | JPS5127242B1 (en) |
AR (1) | AR220881A1 (en) |
AU (1) | AU458034B2 (en) |
BR (1) | BR7204613D0 (en) |
CA (1) | CA978126A (en) |
ES (1) | ES404746A1 (en) |
FR (1) | FR2145546B1 (en) |
GB (1) | GB1391649A (en) |
IL (1) | IL39832A (en) |
IT (1) | IT965901B (en) |
NL (1) | NL7209605A (en) |
PL (1) | PL89010B1 (en) |
SE (1) | SE373833B (en) |
SU (1) | SU506302A3 (en) |
ZA (1) | ZA724588B (en) |
Families Citing this family (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3882014A (en) * | 1972-10-26 | 1975-05-06 | Universal Oil Prod Co | Reaction zone effluents separation and hydrogen enrichment process |
US3847796A (en) * | 1973-03-15 | 1974-11-12 | Universal Oil Prod Co | Hydrocracking process for the production of lpg |
US3917562A (en) * | 1974-07-16 | 1975-11-04 | Universal Oil Prod Co | Combination process for the conversion of heavy distillates to LPG |
US3963600A (en) * | 1974-07-16 | 1976-06-15 | Universal Oil Products Company | Combination process for the conversion of heavy distillates to LPG |
US4247386A (en) * | 1979-08-06 | 1981-01-27 | Mobil Oil Corporation | Conversion of hydrocarbons to olefins |
JPS6238179U (en) * | 1985-08-26 | 1987-03-06 | ||
GB2195654A (en) * | 1986-09-30 | 1988-04-13 | Shell Int Research | Process for recovery of hydrocarbons from a fluid feed |
US4875991A (en) * | 1989-03-27 | 1989-10-24 | Amoco Corporation | Two-catalyst hydrocracking process |
US6379533B1 (en) * | 2000-12-18 | 2002-04-30 | Uop Llc | Hydrocracking process for production of LPG and distillate hydrocarbons |
MY135793A (en) | 2002-07-12 | 2008-06-30 | Basf Ag | Method for the production of butadiene from n-butane |
US6953870B2 (en) * | 2002-08-26 | 2005-10-11 | Tsoung Y Yan | Self-propelled liquid fuel |
US8926826B2 (en) * | 2011-04-28 | 2015-01-06 | E I Du Pont De Nemours And Company | Liquid-full hydroprocessing to improve sulfur removal using one or more liquid recycle streams |
SG11201606020PA (en) * | 2014-02-25 | 2016-08-30 | Saudi Basic Ind Corp | Process for converting hydrocarbons into olefins |
CN106062147B (en) * | 2014-02-25 | 2018-07-24 | 沙特基础工业公司 | Method for converting hydrocarbons to alkene |
KR20170098867A (en) | 2014-12-22 | 2017-08-30 | 사빅 글로벌 테크놀러지스 비.브이. | Process for producing c2 and c3 hydrocarbons |
US10087378B2 (en) | 2014-12-22 | 2018-10-02 | Sabic Global Technologies B.V. | Process for producing LPG and BTX |
SG11201704528TA (en) | 2014-12-22 | 2017-07-28 | Sabic Global Technologies Bv | Process for producing lpg and btx |
CN114350408A (en) | 2014-12-22 | 2022-04-15 | 沙特基础工业全球技术有限公司 | Process for producing C2 and C3 hydrocarbons |
EP3390582B1 (en) * | 2015-12-15 | 2024-02-21 | SABIC Global Technologies B.V. | Process for producing c2 and c3 hydrocarbons |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3047490A (en) * | 1958-11-04 | 1962-07-31 | Phillips Petroleum Co | Hydrocracking process |
US3215617A (en) * | 1962-06-13 | 1965-11-02 | Cities Service Res & Dev Co | Hydrogenation cracking process in two stages |
GB1088933A (en) * | 1964-03-10 | 1967-10-25 | British Petroleum Co | Improvements relating to the catalytic conversion of hydrocarbons |
US3256178A (en) * | 1965-05-25 | 1966-06-14 | Union Oil Co | Hydrocracking process |
US3617483A (en) * | 1968-04-25 | 1971-11-02 | Texaco Inc | Hydrocracking process |
US3607723A (en) * | 1969-03-28 | 1971-09-21 | Texaco Inc | Split flow hydrocracking process |
-
1971
- 1971-07-12 US US00161586A patent/US3718575A/en not_active Expired - Lifetime
-
1972
- 1972-07-04 ZA ZA724588A patent/ZA724588B/en unknown
- 1972-07-05 IL IL39832A patent/IL39832A/en unknown
- 1972-07-07 PL PL1972156549A patent/PL89010B1/pl unknown
- 1972-07-10 IT IT51462/72A patent/IT965901B/en active
- 1972-07-10 FR FR7224867A patent/FR2145546B1/fr not_active Expired
- 1972-07-11 GB GB3233572A patent/GB1391649A/en not_active Expired
- 1972-07-11 CA CA146,847A patent/CA978126A/en not_active Expired
- 1972-07-11 AU AU44425/72A patent/AU458034B2/en not_active Expired
- 1972-07-11 SE SE7209137A patent/SE373833B/xx unknown
- 1972-07-11 ES ES404746A patent/ES404746A1/en not_active Expired
- 1972-07-12 AR AR243020A patent/AR220881A1/en active
- 1972-07-12 NL NL7209605A patent/NL7209605A/xx not_active Application Discontinuation
- 1972-07-12 BR BR4613/72A patent/BR7204613D0/en unknown
- 1972-07-12 JP JP47069218A patent/JPS5127242B1/ja active Pending
- 1972-07-12 SU SU1812197A patent/SU506302A3/en active
Also Published As
Publication number | Publication date |
---|---|
FR2145546B1 (en) | 1978-01-06 |
AR220881A1 (en) | 1980-12-15 |
IL39832A (en) | 1975-04-25 |
FR2145546A1 (en) | 1973-02-23 |
PL89010B1 (en) | 1976-10-30 |
JPS5127242B1 (en) | 1976-08-11 |
IT965901B (en) | 1974-02-11 |
NL7209605A (en) | 1973-01-16 |
AU4442572A (en) | 1974-01-17 |
ES404746A1 (en) | 1975-07-01 |
IL39832A0 (en) | 1972-09-28 |
GB1391649A (en) | 1975-04-23 |
DE2233826B2 (en) | 1975-11-13 |
AU458034B2 (en) | 1975-02-13 |
SE373833B (en) | 1975-02-17 |
DE2233826A1 (en) | 1973-02-08 |
BR7204613D0 (en) | 1973-05-24 |
ZA724588B (en) | 1973-04-25 |
US3718575A (en) | 1973-02-27 |
CA978126A (en) | 1975-11-18 |
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