200829689 九、發明說明： 【發明所屬之技術領域】 本發明大體而言係關於烴處理，且更特定言之係關於處 理諸如在重烴原料之裂解中或藉由重烴原料之裂解生成或 幵> 成之具有高輕烯烴含量的含烴物質。 【先前技術】 輕烯烴在許多化學品製造中用作饋入材料。輕烯烴傳統 上藉由諸如石油來源所衍生之烴之蒸汽或催化裂解的製程 來製造。重烴流之流體化性催化裂解（FCC)通常藉由使起 始物負（無淪其為真空製氣油、蒸餾原油或相關高沸點烴 之另一來源）與諸如由細粉狀或微粒固體物質組成之催化 劑接觸來進行。藉由以足以產生所要流體輸送狀況之速度 傳輸氣體或蒸氣通過催化劑來以類流體方式輸送該催化 劑。油與流體化物質之接觸催化裂解反應。 裂解反應通常使焦炭沈積於催化劑上。離開反應區之催 化劑通常稱作"廢催化劑"，亦即由於焦炭沈積於催化劑上 而部分去活化。焦炭由氫及碳組成且可包括痕量之其他物 質’諸如可與起始物質一起進入製程之硫及金屬。焦炭之 存在干擾廢催化劑之催化活性。咸信焦炭阻斷催化劑表面 上裂解反應發生的酸位點。傳統上將廢催化劑轉移至自催 化劑移除吸附烴及氣體之汽提器且接著轉移至再生器以便 藉由用含氧氣體氧化來移除焦炭。收集相對於汽提器中之 廢催化劑而言具有降低之焦炭含量之催化劑的總量（下文 稱作再生催化劑）用於返回反應區。氧化來自催化劑表面 125173.doc 200829689 之焦厌釋放大量熱，其之一部分與一般稱作廢氣之焦炭氧 化之氣體產物一起逸出再生器。其餘熱與再生催化劑一起 離開再生器。流體化催化劑在反應區與再生區之間連續循 壞。流體化催化劑（其亦提供催化功能）用作熱在區與區之 間轉移之媒劑。在丁agam〇lila等人之美國專利5,36〇,533、 L〇maS之美國專利5,5料，985、Castillo之美國專利5,858,206 及Eng之美國專利6,843,9〇6 B1中更全面描述FCC處理，此 等專利之各者之内容以引用的方式併入本文中。熟習此項 技術者熟知各種接觸區、再生區及汽提區連同在各種區之 間傳送催化劑之設備的特定細節。 FCC反應器用於使柴油或重饋料裂解成範圍廣泛之產 品。來自FCC裝置之裂解蒸氣進入通常為主塔形式之分離 區，其提供氣流、汽油餾份、輕循環油（LC〇)及包括重循 環油（HC0)組份之澄清油（c〇)。該氣流可包括乾氣，亦即 氫及(^及^烴；及液化石油氣（”LpG”），亦即^及^烴， 有時亦稱作濕氣。 考慮到對用於各種石油化學用途（諸如用於生產聚乙 烯、聚丙烯及其類似物）之諸如乙烯及丙烯之輕烯烴日益 增長的需求，以及想要生產相對較少之通常出於環境考慮 而不欲為汽油摻合組份的諸如丁烯及戊烯之重烯烴，可能 想要實施重烴原料之裂解反應處理以增加所得產品構成中 輕烯烴之相對量。 研究成果已導致生成或造成輕烯烴（亦即乙烯及丙烯）產 量相對提高的FCC製程之發展。該處理在^“瓜⑽等人之美 125173.doc -10- 200829689 国專利6,538，169 B1中更完整地描述，該專利内容以 之方式全部併入本文中。 搜相仏t 如及导利所揭不，可使烴進料流 觸V、包含再生催化劑及焦炭化催化劑之摻合催化劑接 觸。该催化劑具有包括第一組份及第二植份之組合物。： 含具有不大於中等孔隙尺寸之彿石，丨中該彿石 、，M組合物之至少1重量％。接觸發生於一上升管中 裂解進料㈣中之煙且獲得含有包括輕婦煙及焦炭化催化200829689 IX. INSTRUCTIONS OF THE INVENTION: TECHNICAL FIELD OF THE INVENTION The present invention relates generally to hydrocarbon processing, and more particularly to treatments such as in cracking of heavy hydrocarbon feedstocks or by cracking of heavy hydrocarbon feedstocks or > A hydrocarbon-containing material having a high light olefin content. [Prior Art] Light olefins are used as feed materials in the manufacture of many chemicals. Light olefins are traditionally manufactured by processes such as steam or catalytic cracking of hydrocarbons derived from petroleum sources. Fluid catalytic cracking (FCC) of heavy hydrocarbon streams is usually carried out by making the starting material negative (no other gas source for vacuum, distilled crude oil or another source of related high boiling hydrocarbons) and such as by fine powder or fine particles. The catalyst of the solid matter composition is brought into contact. The catalyst is fluid-likely delivered by passing a gas or vapor through the catalyst at a rate sufficient to produce the desired fluid delivery condition. The contact of the oil with the fluidized material catalyzes the cleavage reaction. The cleavage reaction typically deposits coke on the catalyst. The catalyst leaving the reaction zone is commonly referred to as "waste catalyst", i.e., partially deactivated due to coke deposition on the catalyst. Coke is composed of hydrogen and carbon and may include traces of other materials such as sulfur and metals that may enter the process with the starting materials. The presence of coke interferes with the catalytic activity of the spent catalyst. The salt coke blocks the acid sites at the surface of the catalyst. The spent catalyst is conventionally transferred to a self-catalyst to remove a stripper that adsorbs hydrocarbons and gases and then transferred to a regenerator to remove coke by oxidation with an oxygen-containing gas. The total amount of catalyst (hereinafter referred to as regenerated catalyst) having a reduced coke content relative to the spent catalyst in the stripper is collected for return to the reaction zone. Oxidation from the catalyst surface 125173.doc 200829689 releases a large amount of heat, some of which escapes the regenerator together with the gaseous product of the coke oxidized, generally referred to as exhaust gas. The remaining heat leaves the regenerator along with the regenerated catalyst. The fluidized catalyst continuously circulates between the reaction zone and the regeneration zone. The fluidized catalyst (which also provides a catalytic function) acts as a vehicle for the transfer of heat between zones. It is more fully described in U.S. Patent No. 5,36,533 to D. A., et al., U.S. Patent No. 5,5, the entire disclosure of which is incorporated herein by reference. FCC processing, the contents of each of which are incorporated herein by reference. Specific details of various contact zones, regeneration zones and stripping zones, as well as equipment for transporting catalysts between zones, are well known to those skilled in the art. FCC reactors are used to crack diesel or heavy feedstock into a wide range of products. The cracked vapor from the FCC unit enters a separation zone, typically in the form of a main column, which provides a gas stream, a gasoline fraction, a light cycle oil (LC®), and a decant oil (c〇) comprising a heavy cycle oil (HC0) component. The gas stream may include dry gas, that is, hydrogen and (and hydrocarbons; and liquefied petroleum gas ("LpG"), that is, hydrocarbons, sometimes referred to as moisture. Considering the use of various petrochemicals Uses such as the growing demand for light olefins such as ethylene and propylene for the production of polyethylene, polypropylene and the like, and the desire to produce relatively small amounts of gasoline blending that are generally not environmentally desirable. Parts of heavy olefins such as butenes and pentene may be subjected to a cracking reaction treatment of heavy hydrocarbon feedstocks to increase the relative amount of light olefins formed in the resulting product. Research results have led to the formation or formation of light olefins (ie, ethylene and propylene). The development of a relatively high-yield FCC process. This process is more fully described in the U.S. Patent No. 125,173. doc -10- 200829 689, the entire disclosure of which is incorporated herein by reference. The search phase can be contacted with a blending catalyst comprising a regenerated catalyst and a coked catalyst, as disclosed in the disclosure. The catalyst has a combination comprising a first component and a second plant. Object Containing at least 1% by weight of the Fossil, M composition of the Fossil, M composition. Contact occurs in a rising tube to crack the smoke in the feed (4) and obtains the inclusion of light smoke And coke catalysis
，產物之料流。使裂解流通過該上升管之-端流出 得;^進料机在上升管中與摻合催化劑接觸平均少於或 專於2秒。 考慮到對諸如乙烯及丙烯之輕烯烴日益增長之需求，需 ;自口亥FCC製程流出物分離及回收輕烯烴的改良之方 法及設備。 【發明内容】 本t明之一般目標為提供用於催化裂解重烴原料且獲得 所選烴餾份之改良之方法及系統。 、本發明之一般目標可至少部分藉由特定方法達成，該方 ，諸如包括使重烴原料與烴裂解催化劑在一流體化反應器 區中接觸以生成包含一系列包括輕烯烴之裂解烴產物的烴 流出物。根據一較佳實施例，烴裂解催化劑理想地為包括 包含大孔分子篩的第一組份及一包含具有不大於中等孔 隙尺寸之沸石的第二組份之組合物，其中該具有不大於中 等孔隙尺寸之沸石佔催化劑組合物之至少1 · 〇重量％。使烴 /瓜出物在刀離4又中分離以形成至少一分離器液流及一分離 125173.doc 200829689 器蒸氣流。該至少一分離器液流包括c3+烴。該分離器蒸 氣流包括Cy烴。使分離器蒸氣流與第一吸收溶劑在吸收 區中接觸以自其移除（：3+烴且形成包括c2_烴物質之製程 流。可理想地自該至少一分離器液流中汽提c2_烴物質以 形成大體上無Cr烴之C3 +烴製程流。將c5 +烴物質自c3 +烴 製程流中分離以形成包括C5+烴物質之第一產物製程流及 包括C3及C4烴之第二產物製程流。理想地將第一產物流之 至少第一部分引入吸收區作為第一吸收溶劑之至少一部 分。 先前技術一般未能提供以可能需要之卓有成效之方式經 由重烴原料之催化裂解獲得輕烯烴的處理流程及設備。更 特定言之，先前技術一般未能提供該等有利地利用基於吸 收之產物回收來生成或另外獲得含有特定所要範圍之烴之 製程流的處理流程及設備。 根據另一實施例，一種用於催化裂解重烴原料且獲得所 選烴餾份之方法包括使重烴原料與包括再生催化劑及焦炭 化催化劑之摻合裂解催化劑在一流體化反應器區中於烴裂 解反應條件下接觸以生成包括U包括輕婦烴之煙產物 的烴流出物流。催化劑理想地為包括包含大孔分子篩之第 一組份及包含具有不大於中等孔隙尺寸之沸石之第二組份 的組合物。該具有不大於甲等孔隙尺寸之沸石佔該催化劑 組合物之至少1 · 0重量％。 該方法進-步包括在一分離區中分離烴流出物以形成至 少一分離器高壓液流及一分離器高壓蒸氣流。該至少一分 125173.doc 200829689 離器高壓液流包含C3+烴。該分離器高壓蒸氣流包含c3_ 烴。使分離器高壓蒸氣流與第一吸收溶劑在一初級吸收器 中接觸以形成包括主要Cr烴及殘餘量之C3 +烴的第一初級 吸收器製程流。使第一初級吸收器製程流與第二吸收溶劑 接觸以形成包括Cy烴物質之製程流及包括殘餘c3 +烴及第 二吸收溶劑之製程流。自分離器高壓液流中汽提Cr烴物 質以形成大體上無Cr烴之c：3 +烴製程流。自c3 +烴製程流 分離C5 +烴物質以形成包括C5 +烴物質之第一產物製程流及 包括C3及C4烴之第二產物製程流。該方法進一步包括將第 一產物流之至少第一部分引入初級吸收器作為大量第一吸 收溶劑。 亦提供一種用於催化裂解重烴原料且獲得所選烴餾份之 系、、先根據較佳實施例，該系統包括一流體化反應器 區，其中重烴原料在烴裂解反應條件下接觸包括再生催化 劑及焦炭化催化劑之摻合催化劑以生成含有包括輕烯烴之 烴產物的裂解流出物流。 該系統亦包括一分離區’其用於分離裂解流出物流以形 成至少一分離器液流及分離器蒸氣流。該至少一分離器液 流包含C3+烴。該分離器蒸氣流包含c3_烴。 該系統進-步包括一吸收區’用以自分離器高壓蒸氣流 吸收C3 +烴於第一吸收溶劑中且形成包括包含乙烯之匸2-烴 的吸收區流出物流。提供一汽提器，用於自分離器液流中 汽提C2-烴物質以形成大體上無C2·烴之製程流。提供 一去丁烷塔，用於自Cs+烴製程流分離C5+烴物質以形成包 125173.doc 200829689 括⑽物質t第一製程流及包括^及。烴之第二製程 流。該系統亦包括-製程管線，用於將第一產物流之至少 第一部分引入吸收區作為大量第一吸收溶劑。 如本文所使用，提及之”輕烯烴”理解為一般係指單獨或 組合之C2及C3烯烴，亦即乙稀及丙烯。, the product stream. The cleavage stream is passed through the end of the riser; the feeder is contacted with the admixture catalyst in the riser on average less than or exclusively for 2 seconds. In view of the growing demand for light olefins such as ethylene and propylene, there is a need for improved methods and equipment for the separation and recovery of light olefins from the FCC process effluent. SUMMARY OF THE INVENTION A general object of the present invention is to provide an improved method and system for catalytically cracking heavy hydrocarbon feedstocks and obtaining selected hydrocarbon fractions. The general object of the present invention can be at least partially achieved by a specific process, such as comprising contacting a heavy hydrocarbon feedstock with a hydrocarbon cracking catalyst in a fluidized reactor zone to produce a cracked hydrocarbon product comprising a series of light olefins. Hydrocarbon effluent. According to a preferred embodiment, the hydrocarbon cracking catalyst desirably comprises a composition comprising a first component comprising a macroporous molecular sieve and a second component comprising a zeolite having a size no greater than a medium pore size, wherein the hydrocarbon cracking composition has no greater than medium porosity The size of the zeolite comprises at least 1% by weight of the catalyst composition. The hydrocarbon/melon extract is separated in a knife separation to form at least one separator stream and a separator vapor stream. The at least one separator stream comprises c3+ hydrocarbons. The separator vapor stream comprises a Cy hydrocarbon. Separating the separator vapor stream from the first absorption solvent in the absorption zone to remove therefrom (: 3+ hydrocarbons and forming a process stream comprising the c2_hydrocarbon species. Ideally stripping from the at least one separator stream C2_hydrocarbon material to form a C3+ hydrocarbon process stream substantially free of Cr hydrocarbons. The c5+ hydrocarbon material is separated from the c3+ hydrocarbon process stream to form a first product process stream comprising C5+ hydrocarbon species and comprising C3 and C4 hydrocarbons a second product process stream. Ideally introducing at least a first portion of the first product stream into the absorption zone as at least a portion of the first absorption solvent. The prior art generally fails to provide a catalytic cracking of the heavy hydrocarbon feedstock in a manner that may be required in a fruitful manner. Processes and equipment for the treatment of light olefins. More specifically, prior art techniques generally fail to provide such process flows and equipment that advantageously utilize absorption based product recovery to generate or otherwise obtain a process stream containing hydrocarbons of a particular desired range. In another embodiment, a method for catalytically cracking a heavy hydrocarbon feedstock and obtaining a selected hydrocarbon fraction comprises reacting a heavy hydrocarbon feedstock with a regenerated catalyst and a coked catalyst The blending cracking catalyst is contacted in a fluidized reactor zone under hydrocarbon cracking reaction conditions to form a hydrocarbon effluent stream comprising U including a chiral hydrocarbon product. The catalyst desirably comprises a first component comprising a macroporous molecular sieve and a composition comprising a second component of zeolite having a size greater than a medium pore size. The zeolite having a pore size no greater than the pore size of the catalyst comprises at least 1.0% by weight of the catalyst composition. The method further comprises a separation The hydrocarbon effluent is separated in the zone to form at least one separator high pressure liquid stream and a separator high pressure vapor stream. The at least one minute 125173.doc 200829689 off-higher liquid stream comprises C3+ hydrocarbons. The separator high pressure vapor stream comprises c3_hydrocarbons. The separator high pressure vapor stream is contacted with a first absorption solvent in a primary absorber to form a first primary absorber process stream comprising a primary Cr hydrocarbon and a residual amount of C3+ hydrocarbons. The first primary absorber process stream is first The second absorption solvent contacts to form a process stream comprising the Cy hydrocarbon material and a process stream comprising residual c3 + hydrocarbons and a second absorption solvent. Stripping the Cr hydrocarbons from the high pressure liquid stream of the separator To form a c:3 + hydrocarbon process stream substantially free of Cr hydrocarbons. The C5 + hydrocarbon material is separated from the c3 + hydrocarbon process stream to form a first product process stream comprising a C5 + hydrocarbon material and a second stream comprising C3 and C4 hydrocarbons a product process stream. The method further comprises introducing at least a first portion of the first product stream to the primary absorber as a plurality of first absorption solvents. Also providing a system for catalytically cracking a heavy hydrocarbon feedstock and obtaining a selected hydrocarbon fraction, According to a preferred embodiment, the system includes a fluidized reactor zone in which a heavy hydrocarbon feedstock is contacted with a blended catalyst comprising a regenerated catalyst and a coked catalyst under hydrocarbon cracking reaction conditions to produce a cracked effluent comprising a hydrocarbon product comprising light olefins The system also includes a separation zone for separating the cracked effluent stream to form at least one separator stream and a separator vapor stream. The at least one separator stream comprises C3+ hydrocarbons. The separator vapor stream contains c3_hydrocarbons. The system further includes an absorption zone' for absorbing C3+ hydrocarbons from the separator high pressure vapor stream in the first absorption solvent and forming an absorption zone effluent stream comprising ethylene-containing hydrocarbons. A stripper is provided for stripping the C2-hydrocarbon species from the separator stream to form a substantially C2-free hydrocarbon process stream. A debutanizer column is provided for separating C5+ hydrocarbon species from the Cs+ hydrocarbon process stream to form a package 125173.doc 200829689 comprising (10) a first process stream of material t and comprising. The second process stream of hydrocarbons. The system also includes a process line for introducing at least a first portion of the first product stream into the absorption zone as a plurality of first absorption solvents. As used herein, reference to "light olefin" is understood to mean generally C2 and C3 olefins, i.e., ethylene and propylene, alone or in combination.
提及之輕烯烴物質或適當製程流"大體上無二氧化碳"理 解為-般係指該等輕烯烴物f或製程流理想地—般含有小 於約1〇〇 PPm之二氧化碳，較佳含有小於約io ppm之二氧 化碳且更佳理想地含有小於約！ ppm之二氧化碳。 提及之製程流"富含乙婦"理解為一般係指該等製程流一 般含有至少2G%乙烯且根據至少特定較佳實施例或者含有 至少25%乙浠、至少3G%乙烯、至少35%乙婦、至少4〇%乙 烯或約40%至約60%乙烯。 提及之"CXM，，理解為係指具有由下標，，χ"表示之碳原子數 之烴分子。類似地’術語"含Cx之物流"係指含有&煙之物 流。術語”Cx+烴"係指具有由下標，，χ"或大於"χ”表示之碳原 子數之烴分子。例如，"C4+煙"包括C4、c5及更高碳數之 烴。術語"Cx-烴"係指具有由下標,,χΙ，或小於,,χ„表示之碳原 子數之烴分子。例如，” Γ 、咕> 门 C4_fe包括C4、c3及更低碳數之 烴0 自以下實施方式連同隨时請專利範圍及圖式，其他目 標及優點對於熟習此項技術者而言為顯^見的。 【實施方式】 提ί、I:由k衣解處理來卓有成效地處理重烴原料的處理 125173.doc -14- 200829689 流程及設備，其中所選烴餾份係經由基於吸收之產物回收 獲得。 根據本發明之一實施例，該圖示意性說明一般由參考數 字210表示的一系統，其用於催化裂解重烴原料且經由基 於吸收之產物回收獲得輕烯烴。熟習此項技術者及由本文 提供之教示所導引者將認識且瞭解到所說明之系統已藉由 排除各種常見或習知製程設備部件（包括某些熱交換器、 製程控制系統、泵、分餾系統及其類似物）而簡化。亦可 暸解圖中所描繪之製程流可在不偏離本發明之基本總概念 的情況下在許多方面進行修改。 在系統210中，將合適重烴原料流經由一管線212引入一 流體化反應器區214，其中該重烴原料與一烴裂解催化劑 區接觸以生成包含一系列包括輕烯烴之烴產物的烴流出 物0 用於實施該實施例之合適流體化性催化裂解反應器區巧 (如上述阳_等人之美國專利6,538，169 m中所述）包和 刀離态谷盗、一再生窃、一摻合容器及一提供於其中潑 生轉化：空氣傳送區之垂直上升管。該設備使催化劑循拜 且以特定描述之方式接觸饋料。 一=定言之^如本文所述，催化劑通常包含兩種可在同 基貝上或可不在同一基質上 個系統而循環。第一且…該兩種組份遍及整 、、々匕括任何用於流體化性催化裂 解技術中之熟知催化劑，諸如 或高活性結晶分子冑黏土型催化劑及/ 子師0刀子師催化劑優於非晶形催化劑， 125173.doc 200829689 因為其對所要產物具更加改良之選擇性。在fcc製程中， ’弗石為最常用之分子篩。第一催化劑組份較佳包含大孔滞 石’諸如γ-型彿石、活性氧化銘物質、包含二氧化石夕或氧 化鋁之黏合劑物質及諸如高嶺土之惰性填料。 、適用於第-催化劑組份之沸石分子篩應具有大的平均孔 隙尺寸。通常’具有大孔隙尺寸之分子篩具有以大於1〇且 通常12員環所界定之有效直徑大於^⑽之開口的孔。大 孔之孔隙尺寸指數大於約31。合適大孔滞石組份包括合成 滞石’諸如X-型及γ_型涛石、絲光彿石及八面彿石。已發 現具有低稀土含量之γ滞石在第一催化劑組份中為較佳。 低稀土含量表示在催化劑之沸石部分上有小於或等於約 1.0重量％稀土氧化物。由w. R. Grace & c〇.所製之 Octacat μ催化劑為合適低稀土之沸石催化劑。 第二催化劑組份包含含有由ZSM_5、ZSM_u、zsm_ =、讀-23、ZSM_35、ZSM_38、纖,及其他類似物 質所例示之中等或較小孔之沸石催化劑的催化劑。美國專 利第3,702,886號描述ZSM-5。其他合適中等或較小孔之沸 石包括鎂鹼沸石、毛沸石及由Petr〇le〇s心S.A. 開發之ST-5。第二催化劑組份較佳將中等或較小孔之沸石 分散於一包含諸如二氧化石夕或氧化銘之黏合劑物質及諸如 高嶺土之惰性填料之基質上。第二組份亦可包含某些其他 活性物質，諸如β沸石。此等催化劑組合物具有^ Ο —。重量 %或更多之結晶沸石含量及75_90重量％之基質物質含量。 含有25重量％結晶沸石物質之催化劑為較佳。可使用具有 125173.doc •16- 200829689 =晶沸石，量之催化劑，限制條件為其具有令人滿意 而…性°㈠及較小孔之$石之特徵為具有小於或等於 〇. 7 nm之有效孔開口直徑、1卩昌 且仫10貝或10員以下之環及小於31 之孔隙尺寸指數。 總催化劑組合物應含有〇番旦 另i()重里％之中等至小孔沸石， 其中大於或等於1.75重量％為較佳。告 田弟一催化劑組份含Reference to a light olefinic material or a suitable process stream "substantially free of carbon dioxide" is understood to mean that such light olefins or process streams desirably contain less than about 1 〇〇 ppm of carbon dioxide, preferably containing Less than about io ppm of carbon dioxide and more preferably ideally less than about! Carbon dioxide in ppm. The process flow referred to "enriched " is generally understood to mean that the process streams generally contain at least 2 G% ethylene and according to at least certain preferred embodiments or contain at least 25% acetamidine, at least 3 G% ethylene, at least 35% female, at least 4% ethylene or from about 40% to about 60% ethylene. The reference to "CXM," is understood to mean a hydrocarbon molecule having the number of carbon atoms represented by the subscript, χ". Similarly, the term "Cx-containing logistics" refers to a stream containing & The term "Cx+hydrocarbon" means a hydrocarbon molecule having a number of carbon atoms represented by a subscript, χ" or greater than "χ. For example, "C4+smoke" includes hydrocarbons of C4, c5 and higher carbon numbers. The term "Cx-hydrocarbon" refers to a hydrocarbon molecule having a number of carbon atoms represented by a subscript, χΙ, or less than, χ„. For example, Γ, 咕> Gate C4_fe includes C4, c3, and lower Carbon Numbers of Hydrocarbons 0 From the following embodiments, along with the scope and drawings of the patents, other objects and advantages will be apparent to those skilled in the art. [Embodiment] The treatment of a heavy hydrocarbon feedstock is efficiently treated by k-solution treatment. 125173.doc -14- 200829689 The process and equipment wherein the selected hydrocarbon fraction is recovered via absorption-based product recovery. In accordance with an embodiment of the present invention, the figure schematically illustrates a system, generally indicated by reference numeral 210, for catalytically cracking a heavy hydrocarbon feedstock and recovering light olefins via absorption based product recovery. Those skilled in the art and as taught by the teachings provided herein will recognize and appreciate that the systems described have been eliminated by the various common or conventional process equipment components (including certain heat exchangers, process control systems, pumps, The fractionation system and its analogs are simplified. It can also be appreciated that the process flow depicted in the figures can be modified in many respects without departing from the basic general concepts of the invention. In system 210, a suitable heavy hydrocarbon feed stream is introduced via a line 212 to a fluidized reactor zone 214 wherein the heavy hydrocarbon feedstock is contacted with a hydrocarbon cracking catalyst zone to produce a hydrocarbon effluent comprising a series of hydrocarbon products including light olefins. 0 is a suitable fluidized catalytic cracking reactor zone for the implementation of this embodiment (as described in U.S. Patent No. 6,538,169, the entire disclosure of which is incorporated herein by reference). The blending vessel and a vertical riser are provided therein for the conversion: air transfer zone. The apparatus allows the catalyst to follow and contact the feed in a manner specifically described. A = As stated herein, the catalyst typically comprises two systems which may or may not be on the same substrate. First and foremost, the two components are comprehensive, including any of the well-known catalysts used in fluid catalytic cracking techniques, such as or high activity crystalline molecular 胄 clay type catalysts and / Amorphous catalyst, 125173.doc 200829689 because of its improved selectivity to the desired product. In the fcc process, 'Furstone is the most commonly used molecular sieve. The first catalyst component preferably comprises macroporous stones such as gamma-type fossils, active oxidized materials, binder materials comprising cerium oxide or aluminum oxide, and inert fillers such as kaolin. Zeolite molecular sieves suitable for the first catalyst component should have a large average pore size. Typically, a molecular sieve having a large pore size has pores having an effective diameter greater than 1 〇 and usually defined by a 12-membered ring greater than ^(10). The pore size index of the macropores is greater than about 31. Suitable large pore stagnation components include synthetic staghorns such as X-type and gamma-type sapphire, mercerized buddha and octahedron. It has been found that gamma stagnation having a low rare earth content is preferred in the first catalyst component. The low rare earth content means that there is less than or equal to about 1.0% by weight of the rare earth oxide on the zeolite portion of the catalyst. The Octacat μ catalyst prepared by w. R. Grace & c〇. is a suitable low rare earth zeolite catalyst. The second catalyst component comprises a catalyst comprising a zeolite catalyst having a medium or smaller pore exemplified by ZSM_5, ZSM_u, zsm_ =, read-23, ZSM_35, ZSM_38, fiber, and the like. ZSM-5 is described in U.S. Patent No. 3,702,886. Other suitable medium or smaller pore zeolites include ferrierite, erionite and ST-5 developed by Petr〇le〇s S.A. The second catalyst component preferably disperses the medium or smaller pore zeolite in a matrix comprising a binder material such as silica dioxide or oxidized and an inert filler such as kaolin. The second component may also contain certain other active materials such as zeolite beta. These catalyst compositions have ^ Ο -. The crystalline zeolite content of % by weight or more and the matrix matter content of 75 - 90% by weight. A catalyst containing 25% by weight of a crystalline zeolite material is preferred. It is possible to use a catalyst having 125173.doc •16-200829689 = zeolitic zeolite in an amount which is satisfactory and has a characteristic (a) and a smaller pore of $ stone characterized by having a value of less than or equal to 〇. 7 nm. The effective pore opening diameter, the ring of 1 卩 仫 and 仫 10 Å or less, and the pore size index of less than 31. The total catalyst composition should contain a fine fraction of the fine pore zeolite, wherein greater than or equal to 1.75 wt% is preferred. Tell Tiandi a catalyst component
有2 5重1 %結晶彿石時，該έ人J 茨組合物含有4_40重量％之第二 催化劑組份，其中較佳含量為女 各里為大於或等於7重量0/〇。zsm_5 及ST-5型沸石尤其較佳，因為呈 口馮再之阿耐焦炭性將趨於在催 化劑組合物多向通過上升管時保護活性裂解位點，藉此維 持總活性。第-催化劑組份將包含其餘催化劑組合物。在 整個FCC裝置中該催化劑組合物+ $ 口切丫罘及弟二組份之相對 比例大體上不變。 在催化劑組合物之第二組份中中等或較小孔之彿石之高 濃度藉由進-步裂解較輕石腦油範圍分子而改良對輕稀煙 之選擇性。但同時’所得較小濃度之第一催化劑組份仍展 不足夠活性以維持較重饋料分子之轉化至相當高之程度。 因此，適於處理之相對較重饋料包括習知？〇〇原料或較 高沸點或殘餘饋料。通常習知之原料為真空製氣油，其通 常為藉由真空分餾大氣殘餘物所製備之烴物質且其具有 315-622°C(600-1150T)之廣泛沸點範圍，且更通常具有 343-55rC(65(M〇25aF)之較窄沸點範圍。重或殘餘饋料（亦 即沸點高於499°C(930°F)之烴餾份）亦為合適的。本發明之 流體化性催化裂解處理通常很適合於比石腦油範圍之烴 125173.doc -17- 200829689 重、沸點高於177。(3(350卞）之原料。 使流出物或至少其所選部分自流體化反應器區2丨4經由 一管線216進入一諸如包括一主塔段222及一分級壓縮段 224之烴分離系統220。該主塔段222可理想地包括一具有 一相聯之主塔塔頂高壓接收器之主塔分離器，其中流體化 反應|§區流出物可分離成包括諸如通過一管線226之主塔 蒸氣流及諸如通過一管線230之主塔液流的所要餾份。 為便於說明及論述，舉例而言，諸如包括重汽油流、輕 循環油（"LCO")流、重循環油（”hc〇，，）流及澄清油（”c〇”）流 之其他餾份管線在本文中可不展示，在下文中亦不特定描 述。 將主塔蒸氣流管線226引入諸如構建兩級壓縮之分級壓 縮段224中。分級壓縮段224導致形成在一管線232中之高 壓分離器液流及在一管線234中之高壓分離器蒸氣流。雖 然该咼壓液體及高壓蒸氣之壓力可變，但實際上該等物流 通常處於約1375 kPag至約2100 kPag(約200 psig至約300 Psig)範圍内之壓力下。壓縮段224亦可導致形成主要由重 fe物質組成之溢回物質物流且該物流可經由一管線2 %返 回主塔段222。 高壓分離器液流包括C3 +烴且大體上無二氧化碳。高壓 分離器蒸氣流包括（：3_烴且通常包括一定量二氧化碳。 將分離器蒸氣流管線234經由一管線237引入通常由參考 數字236表示之一吸收區。該吸收區236包括一初級吸收器 24〇，其中分離器蒸氣流與由一管線242提供之去丁烷汽油 125173.doc -18- 200829689 物質及由-管線230提供之主塔液流接觸以自至初級吸收 器240之氣體吸收C3 +且分離Q及低彿點餾份。一般而+， 吸收區236包括一初級吸收器，其合適地包括其中間：有 至少一個且較佳兩個或兩個以上中間冷卻器之複數個階級 以幫助達成所要吸收。實際上，該初級吸收器在各對中間 冷卻器間通常包括約5個吸收器階級。因此，根據一較佳 實施例，為達成所要吸收，初級吸收器理想地包括至少約 15個理想階級，在其間適當間隔至少2個中間冷卻器。在 另一較佳實施例中，為達成所要吸收，合適之較佳初級吸 收器理想地包括至少約20個理想階級，在其間適當間隔至 少3個中間冷卻器。在另一較佳實施例中，為達成所要吸 收，合適之較佳初級吸收器理想地包括至少約2〇至約乃個 理想階級’在其間適當間隔4個或4個以上中間冷卻器。雖 然本發明之廣泛實踐未必如此限制，但在至少某些較佳實 施例中已發現有利地使用丙烯作為一或多個該等初級吸收 器之中間冷卻器中之冷卻劑以幫助達成所要吸收。 在去丁烧Ά油及主塔液體中吸收或藉由去丁燒汽油及主 塔液體吸收之C3 +烴可通過一管線243用於根據本發明下文 所述之進一步處理。 來自初級吸收器240之廢氣通過一管線244至一二級或海 綿吸收器246。二級吸收器246使廢氣與來自一管線25〇之 輕循環油接觸。輕循環油吸收大部分剩餘C4及更高碳數烴 且經一管線252返回主分餾器中。C2-烴流作為廢氣自二級 或海綿吸收器246抽取於一管線254中用於下文所述之進一 125173.doc -19- 200829689 步處理。 管線232中之分離器液流及來自管線243之内含物通過一 管線260進入一汽提器262中，該汽提器262移除大部分c2 及較輕氣體於一管線264中。實際上，該汽提器可理想地 在約 1650 kPag至約 1800 kPag(約 240 psig至約 260 psig)範 圍内之壓力下操作，其中在汽提器底部之C2/c3莫耳比小 於〇·〇〇 1且較佳在汽提器底部之CVC3莫耳比小於約〇 〇〇〇2 至約 0.0004。 如所示，在管線264中之C2及較輕氣體可理想地與來自 官線234之高壓分離器蒸氣組合以形成饋入初級吸收器24〇 之官線237。汽提器262經一管線266供應液體c3 +流至一去 丁烷塔270。根據一較佳實施例，合適之該去丁烷塔包括 一冷凝器（未特別展示），該冷凝器理想地在約965 kp叫至 約1105 kPag(約140 psig至約160 psig)之範圍内的壓力下操 作，塔頂中僅有約5莫耳％之匕烴且塔底僅有約5莫耳％之 C4烴。更佳地，塔頂中之Cs烴之相對量小於約卜3莫耳％且 土合底之之相對量小於約1 _3莫耳％。 藉由一管線272將來自去丁烷塔27〇之C3及a烴流在塔頂 取出用於諸如下文所述之進一步處理。一管線274自去丁 烧^ 270 t抽取去丁烧汽油流。根據—較佳實施例，經由 管^2返回至初級吸收器謂之去丁烧汽油流用作其中之 大量第一吸收溶劑。 去丁烷汽油流之另一部分經一管線276通入一石腦油分 125173.doc -20- 200829689 根據一較佳實施例，石腦油分離器280理想地呈諸如其 中安置有一隔離壁281之隔離壁分離塔形式。該隔離壁分 離塔石腦油分離器理想地有效分離引入其中之去丁烷汽油 成包含含有5至6個碳原子之化合物的輕餾份流、包含含有 7至8個碳原子之化合物的中等餾份流及包含含有8個以上 碳原子之化合物的重餾份流。更特定言之，該隔離壁分離 塔可通常於約34 kPag至約1〇4 kPag(約5 psig至約15 psig) 範圍之冷凝器壓力下操作且根據一實施例在約55 kpag至 約85 kPag(約8 psig至約12 psig)之冷凝器壓力下操作。 該等輕、中等及重餾份流適當地分別通過相應管線 282、284及286用於如可需要之進一步處理或產物回收。 回到處理在管線254甲自二級或海綿吸收器246抽取之 Cr烴流，該等物流物質可通過另一壓縮段29〇以形成一管 線292，其通入一壓縮或排出鼓294。該排出鼓294形成通 常由重組份（例如在排出鼓294中液化之仏+烴）及諸如在一 管線296中之抽取物組成之分離流。排出鼓294亦形成主要 包含Cr烴之塔頂流，通常僅有痕量（例如小於i重量％之 C3 +烴，抽取於一管線3〇〇中。 將該管線300中之塔頂流通入一胺處理段3〇2，如此可視 需要實現自其移除C〇2。用於二氧化碳及/或硫化氯移除之 胺處理系統的使用在此項技術中為人熟知。習知之該等胺 處理系統通常使用諸如甲基二乙醇胺_ΕΑ]之胺溶劑來 自煙流物質中I收或以其他方式分離c〇2。4常接著使用 汽提器或再生器以自胺溶劑中汽提經吸收之C02，而允許 125173.doc -21 · 200829689 胺溶劑之再使用。 雖然該胺處理一般經證明對於自各種含烴流中移除二氧 化碳為有效的，但對富含乙烯之烴及含二氧化碳流（諸如 在本發明系統之這點上處理者）應用該胺處理可能會出現 某些不當併發情況，如某些烯烴物質可能會在胺溶劑中或 藉由胺溶劑與c〇2共吸收。該烯烴物質之共吸收不當地減 少可自該處理中回收之輕烯烴的量。此外，在該後續之胺 溶劑的汽提器處理期間，該等烯烴物質之存在會導致聚 合。該聚合會導致胺溶劑之降解且需要昂貴之易地回收處 理。 有鐾於此，可能要求使用諸如包括或合併有插置於胺系 統吸收裔與胺系統汽提器/再生器之間之預汽提器的胺處 理系統。該插置之預汽提器可理想地用於自二氧化碳及胺 洛劑中分離包括諸如乙烯之輕烯烴的烴物質，之後經由再 生器/汽提器進行隨後處理。 使大體上無二氧化碳之含Cr烴之物流通過一管線3〇4至 一乾燥器段306,自其中抽取之水在一管線3〇7中。將含經 A提之烴及可能少量（例如通常小於丨重量％)c〇2的物流經 吕線308傳送（諸如）返回至壓縮段224(諸如）用於（諸如）與 上文所述一致之進一步處理。含有c〇2之物流經一管線3〇9 自胺處理段362傳送。 使大體上無二氧化碳之含乾燥C2_烴之物流通過一管線 310至一乙炔轉化段或裝置320。如此項技術中已知，乙块 轉化段或裝置可使乙炔有效轉化形成乙烯。因在匕，額外之 125173.doc -22- 200829689 西含乙埽之製程流抽取於來自^^轉化段或裝之— 管線322中。 因為乙炔轉化可造成額外形成水，所以可將管線322中 之製程流（若想要）引入可選乾燥裝置324中，諸如自其中抽 取之水在一官線326中且所得乾燥製程流經一管線通入 諸如呈如此項技術中已知用以有效移除c〇2、c〇s、胂及/ 或膦之C〇2、羰基硫化物（"cos”）、胂及/或膦處理器形式 之可選另一處理段332中，抽取物在一管線334中，且經諸 如抽取之處理之物流在一管線336中。 管線336中之經處理物流可理想地引入去甲烧塔34〇中。 根據一較佳實施例，合適之該去曱烧塔包括冷凝器（未特 別展示），該冷凝器理想地在僅約_9〇。〇(-13〇卞）之溫度下、 更佳在約-90°C至約-120°C之範圍之溫度下、較佳在約- 96°C〇130°F至約-150°F，較佳在約-140T)下操作。此外， 用於實踐本發明之較佳去甲烷塔理想地以塔底之甲烷與乙 稀莫耳比僅為約0.0005且更佳塔底之甲烧與乙烯莫耳比僅 為約0.0003至約0.0002來操作。 來自去甲烷塔340之甲烷與氫氣之物流自塔頂經一管線 342取出，諸如用作燃料或若想要用於進一步處理，諸如 送至變壓吸收裝置（未展示）用於H2回收。 一管線344自去曱烷塔340抽取去曱烷物質流。將管線去 甲烧物質344通入一乙浠/乙烧分離器346。根據一較佳實 施例，合適之該乙烯/乙烷分離器包括一冷凝器（未特別展 示），該冷凝器理想地在約1930 kPag至約2105 kPag(約280 125173.doc -23- 200829689 psig至約305 psig)之壓力範圍下操作且理想地操作以使得 在乙烯產物流中僅有約〇·5體積％乙烧，較佳在乙稀產物流 中有小於約〇· 1體積％乙烷且更佳在乙烯產物流中有小於約 〇·〇5體積°/〇乙烷。 該乙烯/乙烷分離器346形成殘餘輕餾份之蒸氣流、乙稀 之部分冷减流及乙烧之塔底流’其分別通過管線3 5 0、3 5 2 及354，用於如此項技術中已知之產物回收或進一步所要 處理。When there are 25% by weight of 1% crystalline fossil, the sputum composition contains 4-40% by weight of the second catalyst component, wherein the preferred content is greater than or equal to 7 weights per ounce. Zeolites of type zsm_5 and ST-5 are particularly preferred because the refractory properties of the von von von will tend to protect the active cleavage sites as the catalyst composition multi-directionally passes through the riser, thereby maintaining overall activity. The first catalyst component will comprise the remaining catalyst composition. The relative proportions of the catalyst composition + the guttata and the second component were substantially unchanged throughout the FCC unit. The high concentration of medium or smaller pores in the second component of the catalyst composition improves the selectivity to light lean smoke by further cracking the lighter naphtha range molecules. At the same time, however, the resulting smaller concentration of the first catalyst component still exhibits insufficient activity to maintain the conversion of heavier feed molecules to a relatively high degree. Therefore, relatively heavy feeds suitable for processing include conventional ones? 〇〇 Raw material or higher boiling point or residual feed. Commonly used materials are vacuum gas oils, which are typically hydrocarbon materials prepared by vacuum fractionation of atmospheric residues and which have a broad boiling range of 315-622 ° C (600-1150 T), and more typically 343-55 rC. (65 (M〇25aF) has a narrower boiling range. Heavy or residual feeds (i.e., hydrocarbon fractions having a boiling point above 499 ° C (930 ° F)) are also suitable. The fluid catalytic cracking of the present invention The treatment is generally suitable for feedstocks with a weight greater than the naphtha range of 125173.doc -17- 200829689 and a boiling point above 177. (3 (350 卞). The effluent or at least a selected portion thereof is self-fluidizing the reactor zone 2丨4 enters a hydrocarbon separation system 220, such as a main tower section 222 and a staged compression section 224, via a line 216. The main tower section 222 desirably includes a high pressure receiver having an associated main tower overhead The main column separator wherein the fluidization reaction § zone effluent can be separated into a desired fraction including a main column vapor stream such as through a line 226 and a main column stream such as through a line 230. For ease of illustration and discussion For example, including heavy gasoline flow, light cycle oil (" The LCO") flow, heavy cycle oil ("hc〇,") stream and other fraction lines of the clarified oil ("c〇") stream may not be shown herein and are not specifically described below. Line 226 is introduced into a staged compression section 224, such as a two stage compression stage. Staged compression section 224 results in a high pressure separator stream formed in line 232 and a high pressure separator vapor stream in line 234. And the pressure of the high pressure vapor is variable, but in practice the streams are typically at a pressure in the range of from about 1375 kPag to about 2100 kPag (about 200 psig to about 300 Psig). The compression section 224 can also result in the formation of predominantly heavy materials. The overflow material stream is composed and the stream can be returned to the main column section 222 via a line of 2%. The high pressure separator stream comprises C3 + hydrocarbons and is substantially free of carbon dioxide. The high pressure separator vapor stream comprises (: 3 - hydrocarbons and usually includes A quantity of carbon dioxide. The separator vapor stream line 234 is introduced via a line 237 to an absorption zone, generally designated by reference numeral 236. The absorption zone 236 includes a primary absorber 24, wherein the separator vapor Contact with the debutane gasoline 125173.doc -18-200829689 material supplied by a line 242 and the main column stream supplied by the line 230 to absorb C3 + from the gas to the primary absorber 240 and separate the Q and the low point Distillate. Generally, the absorption zone 236 includes a primary absorber suitably including a plurality of stages having at least one and preferably two or more intercoolers to assist in achieving the desired absorption. The primary absorber typically includes about five absorber stages between each pair of intercoolers. Thus, in accordance with a preferred embodiment, the primary absorber desirably includes at least about 15 ideal classes for achieving desired absorption with at least 2 intercoolers spaced therebetween. In another preferred embodiment, a suitable preferred primary absorber desirably includes at least about 20 ideal classes for achieving desired absorption with at least 3 intercoolers spaced therebetween. In another preferred embodiment, a suitable preferred primary absorber desirably includes at least about 2 Torr to about an ideal class' suitably spaced 4 or more intercoolers therebetween for achieving desired absorption. While the broad practice of the invention is not necessarily so limited, it has been found in at least some preferred embodiments that propylene is advantageously employed as a coolant in the intercooler of one or more of the primary absorbers to aid in achieving the desired absorption. The C3 + hydrocarbons absorbed in the de-burning oil and the main column liquid or absorbed by the de-burned gasoline and the main column liquid can be passed through a line 243 for further processing in accordance with the present invention as described below. Exhaust gas from primary absorber 240 passes through line 244 to a secondary or sponge absorber 246. Secondary absorber 246 contacts the exhaust gases with light cycle oil from a line 25 of. The light cycle oil absorbs most of the remaining C4 and higher carbon number hydrocarbons and is returned to the main fractionator via line 252. The C2-hydrocarbon stream is withdrawn as a waste gas from a secondary or sponge absorber 246 in a line 254 for further processing as described below in the steps 125173.doc-19-200829689. The separator stream in line 232 and the contents from line 243 enter a stripper 262 through a line 260 which removes most of the c2 and lighter gases in a line 264. In practice, the stripper is desirably operated at a pressure in the range of from about 1650 kPag to about 1800 kPag (about 240 psig to about 260 psig), wherein the C2/c3 molar ratio at the bottom of the stripper is less than 〇· Preferably, the CVC3 molar ratio at the bottom of the stripper is less than about 〇〇〇〇2 to about 0.0004. As shown, the C2 and lighter gases in line 264 are desirably combined with the high pressure separator vapor from line 234 to form an official line 237 that is fed to the primary absorber 24'. Stripper 262 supplies liquid c3+ to a debutanizer column 270 via a line 266. According to a preferred embodiment, suitably the debutanizer column comprises a condenser (not specifically shown) which desirably ranges from about 965 kp to about 1105 kPag (about 140 psig to about 160 psig). Operating under pressure, there is only about 5 moles of terpene hydrocarbons in the top of the column and only about 5 moles of C4 hydrocarbons at the bottom of the column. More preferably, the relative amount of Cs hydrocarbons in the top of the column is less than about 3 mole % and the relative amount of the soil bottom is less than about 1 to 3 mole %. The C3 and a hydrocarbon streams from the debutanizer column 27 are withdrawn at the top of the column by a line 272 for further processing such as described below. A line 274 is taken from the butyl sinter 270 t to extract the gasoline stream. According to a preferred embodiment, returning to the primary absorber via tube 2 means that the de-burned gasoline stream is used as a substantial amount of the first absorption solvent therein. Another portion of the debutanized gasoline stream is passed through a line 276 to a naphtha fraction 125173.doc -20-200829689. According to a preferred embodiment, the naphtha separator 280 is desirably a partition such as a partition wall 281 disposed therein. Separation tower form. The partition wall separation tower naphtha separator is desirably effective for separating the debutanized gasoline introduced therein into a light fraction stream containing a compound having 5 to 6 carbon atoms, and a medium containing a compound having 7 to 8 carbon atoms. a fraction stream and a heavy fraction stream comprising a compound containing more than 8 carbon atoms. More specifically, the dividing wall separation column can operate at a condenser pressure in the range of from about 34 kPag to about 1 〇 4 kPag (about 5 psig to about 15 psig) and from about 55 kpag to about 85 according to an embodiment. Operate at a condenser pressure of kPag (approximately 8 psig to approximately 12 psig). The light, medium and heavy fraction streams are suitably passed through respective lines 282, 284 and 286, respectively, for further processing or product recovery as may be desired. Returning to the processing of the Cr hydrocarbon stream drawn from the secondary or sponge absorber 246 in line 254, the stream may pass through another compression section 29 to form a line 292 which opens into a compression or discharge drum 294. The discharge drum 294 forms a separate stream that is typically comprised of a recombination component (e.g., hydrazine + hydrocarbons liquefied in discharge drum 294) and an extract such as in line 296. The discharge drum 294 also forms an overhead stream comprising primarily Cr hydrocarbons, typically only trace amounts (e.g., less than 9% by weight of C3 + hydrocarbons, extracted in a line 3 Torr. The top of the line 300 is circulated into one The amine treatment section 3 〇 2, such that C 〇 2 can be removed therefrom as desired. The use of amine treatment systems for the removal of carbon dioxide and/or sulphur chloride is well known in the art. The system typically uses an amine solvent such as methyldiethanolamine to extract from the flue gas or otherwise separate c.2. 4 often followed by stripping or regenerator to strip the absorbed solvent from the amine solvent. C02, while allowing reuse of the amine solvent 125173.doc -21 · 200829689. Although the amine treatment has generally proven to be effective for removing carbon dioxide from various hydrocarbon-containing streams, it is effective for ethylene-rich hydrocarbons and carbon dioxide-containing streams ( The use of this amine treatment, such as at the point of the system of the present invention, may result in some improper concurrency, such as certain olefinic species may be co-absorbed in the amine solvent or by the amine solvent with c〇2. The total absorption of matter is not Locally reducing the amount of light olefins that can be recovered from the treatment. Furthermore, the presence of such olefinic species can result in polymerization during the stripper treatment of the subsequent amine solvent. This polymerization can result in degradation of the amine solvent and is expensive. Easily recycled. In this case, it may be desirable to use an amine treatment system such as a pre-stripper that includes or incorporates an amine stripper/reductor between the amine system and the amine system stripper/regenerator. The pre-stroiler can be desirably used to separate hydrocarbon materials including light olefins such as ethylene from carbon dioxide and amide agents, followed by subsequent treatment via a regenerator/stripper. The stream passes through a line 3〇4 to a dryer section 306 from which the water is extracted in a line 3〇7. The stream containing the hydrocarbons raised by A and possibly a small amount (for example usually less than 丨% by weight) c〇2 will be passed. The line 308 is transferred, for example, back to the compression section 224 (such as) for further processing, such as consistent with the above. The stream containing c〇2 is transferred from the amine treatment section 362 via a line 3〇9. Make substantially no The stream of carbon dioxide containing dry C2_hydrocarbon is passed through a line 310 to an acetylene conversion section or unit 320. As is known in the art, an ethylene conversion section or apparatus can efficiently convert acetylene to form ethylene. .doc -22- 200829689 The process stream of the West Acetate is extracted from the conversion section or the line 322. Since acetylene conversion can cause additional water formation, the process stream in line 322 can be used (if desired Introduced into an optional drying unit 324, such as water extracted therefrom in an official line 326 and the resulting drying process flowing through a line such as is known in the art to effectively remove c〇2, c〇 In another process section 332 of the form s, bismuth and/or phosphine C 〇 2, carbonyl sulfide ("cos"), hydrazine and/or phosphine processor, the extract is in a line 334 and The stream, such as the process of extraction, is in a line 336. The treated stream in line 336 can be desirably introduced into the de-burning tower 34. According to a preferred embodiment, the de-burning tower suitably comprises a condenser (not specifically shown) which is desirably only about _9 Torr. At a temperature of 〇(-13〇卞), more preferably at a temperature of from about -90 ° C to about -120 ° C, preferably from about -96 ° C 〇 130 ° F to about -150 ° F, It is preferably operated at about -140 T). Moreover, preferred demethanizers useful in the practice of the present invention desirably have a methane to ethylene molar ratio of only about 0.0005 at the bottom of the column and more preferably only a methanide to vinyl molar ratio of from about 0.0003 to about 0.0002. To operate. The stream of methane and hydrogen from demethanizer 340 is withdrawn from the top of the column via line 342, such as for use as a fuel or if desired for further processing, such as to a pressure swing absorber (not shown) for H2 recovery. A line 344 draws a stream of deparaffinic material from the dedecane column 340. The line of unburned material 344 is passed to an acetonitrile/acetic acid separator 346. According to a preferred embodiment, suitably the ethylene/ethane separator comprises a condenser (not specifically shown) which desirably ranges from about 1930 kPag to about 2105 kPag (about 280 125173.doc -23-200829689 psig Operating at a pressure range of up to about 305 psig) and ideally operated such that only about 5% 5% by volume of E-bake in the ethylene product stream, preferably less than about 〇·1 vol% of ethane in the ethylene product stream. More preferably, it has less than about 〇·〇5 volume/〇 ethane in the ethylene product stream. The ethylene/ethane separator 346 forms a vapor stream of residual light fraction, a portion of the cold-down stream of ethylene, and an underflow of the bottom of the acetonitrile, which are passed through lines 305, 325, and 354, respectively, for such a technique. The product known in the recovery is recovered or further processed.
回到處理自去丁烷塔270之塔頂經管線272取得之含c3及 C4烴之物流，因為該製程流可含有某些相對顯著量之硫化 氫，所以管線272可理想地通入一硫化物移除處理裝置 3 60，如此項技術中已知，該硫化物移除處理裝置諸如 呈胺處理段形式，諸如形成經一管線362傳輸之處理流。 同時硫化 該處理流之硫化氫含量理想地減少至約2〇 氫經一管線3 64移除。 右需要，則可將處理流管線364引人可選苛性驗或類似 物處理段366,諸如以實現進一步之硫化氫㈣，諸如至 硫化風含量降至1 PPm或1 PPm以下。展示硫化氳經-管線 370自苛性鹼處理段366中移除。 使”有適田減少之硫化氫含量之經處理物流經一管線 ::2通广-硫醇處理段374，諸如以諸如經由如此項技術已 之可丨生鹼冼滌實現自該等物流物質中 醇經一管線376移除。 展不爪 于物“吕線380通入一 C3/C4分離器382。根據 125173.doc -24- 200829689 一較佳實施例，合適之該C^C4分離器包括一冷凝器（未特 別展不）’该冷凝裔理想地在約1650 kPag至約18〇〇 kPag(約240 psig至約260 psig)之範圍之壓力下，較佳在約 1724 kPa(約25 0 psig)之壓力下操作且理想地操作以使得在 塔頂產物流中僅有約5莫耳％ C4，較佳在塔頂產物流中有 小於約1莫耳％ C4且在塔底物流中僅有約5莫耳％ c 3，較佳 在塔底物流中有小於約1莫耳％ C3。Returning to the stream containing c3 and C4 hydrocarbons obtained from the top of the butane column 270 via line 272, since the process stream may contain some relatively significant amount of hydrogen sulfide, line 272 may desirably pass a vulcanization. The material removal treatment device 3 60, as is known in the art, is in the form of an amine treatment section, such as forming a process stream that is transported via a line 362. At the same time, the hydrogen sulfide content of the treatment stream is desirably reduced to about 2 Torr. Hydrogen is removed via a line 3 64. If desired, the process stream line 364 can be introduced to an optional caustic or similar treatment section 366, such as to achieve further hydrogen sulfide (IV), such as to a sulfurized air content of less than 1 PPm or less than 1 ppm. The sulphide sulphide-line 370 is removed from the caustic treatment section 366. The treated stream having the reduced hydrogen sulfide content of the field is passed through a line: 2 galvanic-thiol treatment section 374, such as from such a stream material, such as by a biochemical base such as via such a technique. The medium alcohol is removed via a line 376. The "Lin Line 380" is passed into a C3/C4 separator 382. According to a preferred embodiment of 125173.doc-24-200829689, the C^C4 separator suitably comprises a condenser (not specifically shown). The condensation is desirably from about 1650 kPag to about 18 kPa kPa. Operating at a pressure in the range of from 240 psig to about 260 psig, preferably at a pressure of about 1724 kPa (about 25 psig) and ideally operating such that there is only about 5 mole % C4 in the overhead product stream, Preferably, there is less than about 1 mole % C4 in the overhead product stream and only about 5 mole % c 3 in the bottoms stream, preferably less than about 1 mole % C3 in the bottoms stream.
該Cs/C4分離器382形成（：4+烴流，其通過一管線384諸如 用於如此項技術中已知之產物回收或進一步所要處理。 CVC4分離器382亦形成主要由q烴組成之物流，其通過 一管線3 8 6。 可將該管線386中之物流通入一丙烯/丙烷分離器39〇。 根據-較佳實施例，合適之該丙烷/丙烯分離器理想地操 :以使至少98重量％且較佳至少約99重量％之丙婦回收於 :頂桃中且頂流中之丙埽為至少約99U屯的。 該丙稀/丙炫分離器39〇形成丙稀流及丙烧流，其分別通 過管線392及394，諸如詩如此項技 或進-步所要處理。 物口收 因此，理想地提供處理流程及設備用於經由重煙原料之 催化裂解獲得輕烯烴。更 更特疋吕之，提供有利地利用基於 及收之產物回收之處理户 ^ ^來生成或料形成含有 疋縮要乾圍之烴的製程流。 =缺乏本文未特定揭示之任何元 伤或成份的情況下合 ^輝、、且 k地實^本文中說明性揭示之本發 125173.doc -25- 200829689 明。 雖然在上述詳細說明中已關於本發明之特定較佳實施例 ^述本發明，且已出於說明之目的提出許多細節，但對於 熟習此項技術者而言，顯而易見本發明容許另外之實施例 且可在不背離本發明之基本原則的情況下對本文所述之特 • t細節進行相當多地改變。舉例而言，雖然上文已特定參 照一實施例描述本發明，該實施例中胺處理段3〇2置於另 / 一壓縮段290之下游，但熟習此項技術者及由本文提供之 教不所導引者將瞭解本發明之較廣泛實踐未必受此限制。 此在某些實施例中可需要胺處理段放置於該另一壓縮之上 游。 【圖式簡單說明】 根據一較佳實施例，該圖為用於催化裂解重烴原料且經 由基於吸收之產物回收獲得所選烴餾份（包括輕烯烴）之系 統的簡化示意圖。 # 【主要元件符號說明】 210 糸統 212 管線/重烴原料 214 流體化反應器區 216 管線/烴流出物/裂解流出物流 220 烴分離系統 222 主塔段/分離段 224 分級壓縮段/壓縮段 226 管線/主塔蒸氣流管線 125173.doc -26- 200829689 230 232 234 235 236 237 240 242 243 244 246 250 252 254 260 262 264 266 270 272 274 276 280 281 管線 管線/分離器液流 管線/分離器蒸氣流管線/分離器蒸氣流 管線 吸收區 管線 初級吸收器 管線/第一產物流之第一部分/製程管線 管線 管線 二級吸收器/海綿吸收器 管線 管線 管線/製程流/吸收區流出物流 管線 汽提器 管線 管線/C3 +烴製程流/C3 +製程流 去丁烷塔 管線/第二產物製程流 管線/第一產物製程流 管線/第一產物流之第二部分 石腦油分離器/隔離壁分離塔 隔離壁 125173.doc -27- 200829689 282 管線/輕餾份 284 管線/中等餾份 286 管線/重餾份 290 壓縮段 292 管線 294 壓縮鼓/排出鼓 296 管線 300 管線 302 胺處理段 304 管線 306 乾燥器段 307 管線 308 管線 309 管線 310 管線 320 乙炔轉化段/乙炔轉化裝置 322 管線 324 可選乾燥裝置 326 管線 330 管線 332 處理段 334 管線 33 6 管線 340 去甲烷塔 125173.doc -28- 200829689 342 管線 344 管線/管線去甲烷物質 346 乙烯/乙烷分離器 350 管線 352 管線 354 管線 360 硫化物移除處理裝置 362 管線 364 管線/處理流管線 366 苛性驗處理段 370 管線 372 管線 374 硫醇處理段 376 管線 380 管線 382 C3/C4分離器/C3-C4分離器 384 管線/第二C3-C4分離器製程流 386 管線/第一 C3-C4分離器製程流 390 丙烯/丙烷分離器 392 管線/丙烯製程流 394 管線/丙烷製程流 125173.doc -29-The Cs/C4 separator 382 forms a (:4+ hydrocarbon stream which is passed through a line 384 such as is used for product recovery as is known in the art or further processed. The CVC4 separator 382 also forms a stream consisting essentially of q hydrocarbons, It passes through a line 386. The stream in line 386 can be passed to a propylene/propane separator 39. According to a preferred embodiment, suitably the propane/propylene separator is desirably operated to at least 98 % by weight and preferably at least about 99% by weight of the propylene is recovered in the top peach and the propylene in the top stream is at least about 99 U 。. The propylene/acrylic separator 39 〇 forms a propylene stream and a propylene sinter The flow, which is processed by lines 392 and 394, respectively, such as poetry or advancement. Therefore, it is desirable to provide a process and equipment for obtaining light olefins via catalytic cracking of heavy tobacco feedstock.疋吕之, provides a process stream that advantageously utilizes the treatment of the product based on the recovered product to form or process a hydrocarbon stream containing the collapsed hydrocarbons. = Lack of any elemental damage or composition not specifically disclosed herein. Under the ^ Hui, and k to the real The present invention is described in detail in the foregoing detailed description of the preferred embodiments of the invention, and It will be apparent to those skilled in the art that the present invention is susceptible to additional embodiments and that the details described herein can be varied considerably without departing from the basic principles of the invention. The invention has been described with particular reference to an embodiment in which the amine treatment section 3〇2 is placed downstream of another compression section 290, but those skilled in the art and those taught by the teachings herein will It is to be understood that the broader practice of the invention is not necessarily limited thereto. In some embodiments, an amine treatment section may be required to be placed upstream of the other compression. [Schematic Description] According to a preferred embodiment, the figure is A simplified schematic of a system for catalytically cracking heavy hydrocarbon feedstocks and recovering selected hydrocarbon fractions (including light olefins) via absorption based products. # [Main component symbol description] 210 糸 system 212 Line/heavy hydrocarbon feedstock 214 Fluidization reactor zone 216 Line/hydrocarbon effluent/cracking effluent stream 220 Hydrocarbon separation system 222 Main tower section/separation section 224 Staged compression section/compression section 226 Line/main tower vapor stream line 125173.doc -26- 200829689 230 232 234 235 236 237 240 242 243 244 246 250 252 254 260 262 264 266 270 272 274 276 280 281 Line/separator flow line/separator vapor flow line/separator vapor flow line absorption zone Line Primary Absorber Line / First Product Stream Part 1 / Process Line Line Line Secondary Absorber / Sponge Absorber Line Line Line / Process Flow / Absorption Area Outflow Line Line Stripper Line / C3 + Hydrocarbon Process Stream / C3 + process flow to butane column line / second product process stream line / first product process stream line / second part of first product stream naphtha separator / partition wall separation tower partition wall 125173.doc -27- 200829689 282 Line / Light Fraction 284 Line / Medium Distillation 286 Line / Heavy Fraction 290 Compression Section 292 Line 294 Compression Drum / Drain Drum 296 Line 300 Line 302 Amine Treatment 304 Line 306 Dryer Section 307 Line 308 Line 309 Line 310 Line 320 Ethylene Conversion Section / Acetylene Conversion Unit 322 Line 324 Optional Drying Unit 326 Line 330 Line 332 Treatment Section 334 Line 33 6 Line 340 Demethane Tower 125173.doc -28 - 200829689 342 Line 344 Line/line demethane substance 346 Ethylene/ethane separator 350 Line 352 Line 354 Line 360 Sulfide removal treatment unit 362 Line 364 Line/Processing stream line 366 Causative treatment section 370 Line 372 Line 374 Sulfur Alcohol Treatment Section 376 Line 380 Line 382 C3/C4 Separator / C3-C4 Separator 384 Line / Second C3-C4 Separator Process Stream 386 Line / First C3-C4 Separator Process Stream 390 Propylene / Propane Separator 392 Pipeline / Propylene Process Stream 394 Pipeline / Propane Process Flow 125173.doc -29-