CN100494318C - 用水替代物裂化烃原料的方法 - Google Patents

用水替代物裂化烃原料的方法 Download PDF

Info

Publication number
CN100494318C
CN100494318C CNB038156342A CN03815634A CN100494318C CN 100494318 C CN100494318 C CN 100494318C CN B038156342 A CNB038156342 A CN B038156342A CN 03815634 A CN03815634 A CN 03815634A CN 100494318 C CN100494318 C CN 100494318C
Authority
CN
China
Prior art keywords
stove
water
raw material
mixture
heating
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
CNB038156342A
Other languages
English (en)
Other versions
CN1665908A (zh
Inventor
D·B·司派瑟
A·R·蒂尼克兰托尼奥
J·M·弗莱
R·C·斯特尔
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Chemical Patents Inc
Original Assignee
Exxon Chemical Patents Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US10/188,461 external-priority patent/US7138047B2/en
Priority claimed from US10/188,901 external-priority patent/US7090765B2/en
Priority claimed from US10/189,618 external-priority patent/US7097758B2/en
Application filed by Exxon Chemical Patents Inc filed Critical Exxon Chemical Patents Inc
Publication of CN1665908A publication Critical patent/CN1665908A/zh
Application granted granted Critical
Publication of CN100494318C publication Critical patent/CN100494318C/zh
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/02—Header boxes; End plates
    • F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
    • F28F9/0265—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by using guiding means or impingement means inside the header box
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1022—Fischer-Tropsch products
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1033—Oil well production fluids
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1051—Kerosene having a boiling range of about 180 - 230 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1074—Vacuum distillates
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1077—Vacuum residues
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/80—Additives
    • C10G2300/805—Water
    • C10G2300/807—Steam
    • 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
    • C10G2400/20—C2-C4 olefins

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Lubricants (AREA)
  • Separating Particles In Gases By Inertia (AREA)

Abstract

在炉子中处理烃原料的方法，该方法包括：(a)加热烃原料，(b)向加热的原料中加入水，(c)向加热的原料中加入稀释蒸汽，形成混合物，(d)加热所得混合物并将所得的加热的混合物进料到炉子中，其中(b)中水的加入量为水和稀释蒸汽重量的至少约1%至100%。

Description

用水替代物裂化烃原料的方法
发明背景
发明领域
本发明涉及使用水作为稀释蒸汽的添加物或替代物的烃原料的裂化。
背景技术
利用蒸汽裂化将各种烃原料裂化为烯烃已经有很长时间了。常规的蒸汽裂化采用热解炉，其具有两个主要区域：对流部分和辐射部分反应区。烃原料通常以液体形式(除非以蒸气形式进入的轻原料)进入炉子的对流部分，在此，烃原料通常通过与来自辐射部分的热烟道气间接接触和通过与蒸汽混合而被加热和汽化。然后，汽化的原料和蒸汽混合物进入辐射部分，在此发生裂化。所得的包括烯烃的产物离开热解炉以备进一步的下游处理如骤冷。
非限定性地举例说明，在用于由石脑油原料生产乙烯的常规热解反应炉中，烃原料进入炉子的对流部分，在此烃原料通过与来自辐射部分的炉子烟道气间接接触，在第一换热管中被预热。稀释蒸汽流可以进入对流部分，在此它通过与来自辐射部分的炉子烟道气间接接触，也在换热管中被过热。然后，过热的稀释蒸汽与烃原料混合，以降低在炉子辐射部分的反应区中的烃分压。本领域众所周知，降低在反应区中的烃分压(1)增加了反应器对需要的烯烃产物如乙烯的选择性，和(2)降低了不希望的焦炭形成和沉积在辐射部分管的内表面的速度。过热蒸汽与预热烃原料混合形成汽化烃/蒸汽混合物，该混合物被进一步预热到适合将混合物输送到炉子辐射部分的温度。产生所需的乙烯产物和其它副产物的裂化反应主要在炉子的辐射部分发生。离开辐射部分后，反应器流出物在骤冷系统中被快速冷却，以终止裂化反应。
为了公知的能效目的，希望从离开辐射部分并通过炉子的对流部分流到炉子烟道气排出口的烟道气中回收尽可能多的热。因此，烃原料和稀释蒸汽通常通过与来自辐射部分的烟道气间接接触而在对流部分被加热。对流部分可能还包括其它回收设施，如锅炉给水预热器和/或用于过热高压蒸汽的蒸汽过热器，所述高压蒸汽可以在炉子的骤冷系统中生成。
在有些炉子的设计中，不可能有锅炉给水预热器和/或高压蒸汽过热设施用于从流过对流部分的烟道气流中吸收热量。在这种情况下，烟道气可能在不可接受的高温下排出炉子，例如温度高达600至700℉(315至370℃)。这意味着相当低的能效，因为有些设计使烟道气排出温度低至例如250至300℉(120至150℃)。
在其它情况下，可能希望提供额外的稀释蒸汽以进一步降低烃原料分压。但是这种蒸汽不能以合理的费用得到。
当蒸汽不能另外地以合理的费用得到时，本发明提供了提供额外的稀释蒸汽的优点。
本发明还提供了改善炉子能效的另一个优点。本发明的这些以及其它的特征和优点将从下面的描述和权利要求书中变得显而易见。
发明简述
本发明提供了在炉子中处理烃原料的方法，该方法包括：(a)加热烃原料，(b)向加热的原料中加入水和稀释蒸汽以形成混合物，(c)加热所述混合物，和(d)将来自(c)的加热的混合物进料到炉子中，其中(b)中水的加入量为水和稀释蒸汽重量的至少约1％至100％。在一个实施方案中，水的加入量为水和稀释蒸汽重量的至少约3％(即至少约3％至100％的水)。在另一个实施方案中，水的加入量为水和稀释蒸汽重量的至少约10％。在又一个实施方案中，水的加入量为水和稀释蒸汽重量的至少约30％。根据本发明，水可以是稀释蒸汽的全部替代物(即不加入蒸汽)。然而，优选烃原料中既加入稀释蒸汽又加入水。
根据一个优选的实施方案，水是在加入稀释蒸汽之前加入，如果存在稀释蒸汽的话。
根据另一个实施方案，加入到加热的原料中的水与蒸汽的比例根据至少一个工艺变量的波动来改变。在一个优选的实施方案中，工艺所述变量是工艺温度。在这点上，工艺温度可以是离开炉子的烟道气的温度，炉子对流部分的工艺温度和/或炉子辐射部分(反应区)的工艺温度。
根据又一个实施方案，水在喷雾器中被加入烃原料中，而如果存在稀释蒸汽，稀释蒸汽在另一个喷雾器中被加入原料中。在一个优选的实施方案中，第一和第二喷雾器是喷雾组合装置的部件，在该喷雾组合装置中第一和第二喷雾器以流体流连通方式串联连接。
本发明还提供了在炉子中裂化烃原料的方法，该炉子包括辐射部分和对流部分，所述辐射部分包括产生辐射热和热烟道气的燃烧器，所述对流部分包括换热管，该方法包括：
(a)通过与来自辐射部分的热烟道气间接热交换，在对流部分的换热管中预热烃原料，以提供预热的原料；
(b)在第一喷雾器中向预热的原料中加入水，并在第二喷雾器中向预热的原料中加入稀释蒸汽，以形成原料混合物；
(c)通过与来自辐射部分的热烟道气间接热交换，在对流部分的换热管中加热原料混合物，以形成加热的原料混合物；和
(d)将加热的原料混合物进料到辐射部分，在此加热的原料混合物中的烃被热裂化，以形成产物；
其中(b)中水的加入量为水和稀释蒸汽重量的至少约1％至100％。
在一个优选的实施方案中，第一喷雾器包括被外导管环绕的内部多孔导管，以在内外导管之间形成环流空间。优选地，预热的烃流过环流空间，而水流过内导管并通过内导管上的开口(孔)注入预热的烃原料中。
在又一个优选的实施方案中，第二喷雾器包括被外导管环绕的内部多孔导管，以在内外导管之间形成环流空间。优选地，来自第一喷雾器的原料流过环流空间，而稀释蒸汽流过内导管并通过内导管上的开口(孔)注入第一原料混合物中。
在又一个优选的实施方案中，第一和第二喷雾器是喷雾组合装置的部件，在该喷雾组合装置中第一和第二喷雾器以流体流连通方式串联连接。
附图简述
图1图示说明了根据本发明的采用热解炉的方法的示意流程图，重点在炉子的对流部分。该图还显示了用于根据工艺变量，即进入炉子辐射部分的工艺气体的温度改变水与稀释蒸汽比例的控制简图。图2图示说明了用于根据工艺参数，具体地说离开炉子的烟道气的温度，改变水与稀释蒸汽比例的控制系统的示意图。图3图示说明了相同控制系统的示意图，但是该系统用于根据炉子对流部分中工艺气体的温度来改变水与稀释蒸汽的比例。
发明的详细描述
除非另外指出，所有的百分数、份数、比例等都是以重量为基础。除非另作说明，提到化合物或组分时包括化合物或组分本身，以及与其它化合物或组分的组合如化合物的混合物。
此外，当数量、浓度或其它值或参数以一系列上限优选值和下限优选值给出时，这应当理解为具体公开了上限优选值和下限优选值的任意一对形成的所有范围，不管所述范围是否被单独公开。
本发明涉及在炉子中处理烃原料的方法。根据一个实施方案，该方法包括：(a)加热烃原料，(b)向加热的原料中加入水和稀释蒸汽以形成混合物，(c)加热所述混合物，和(d)将所述加热的混合物进料到炉子中，其中(b)中水的加入量为水和稀释蒸汽重量的至少约1％至100％。
具体参考图1，1总指由下部的辐射部分2、中间的对流部分3和上部的烟道气排出部分4组成的热解炉。在辐射部分中，辐射燃烧器为烃原料提供辐射热，以通过原料的热裂化产生所需要的产物。燃烧器产生热气，该热气向上流过对流部分3，然后通过烟道气排出部分4排出炉子。如图1所示，烃原料33进入对流部分3的上部，在此它被预热。烃原料的预热可以采用本领域普通技术人员所知道的任意形式。然而，优选的是，加热包括原料在炉子1的对流部分3的上部与来自炉子辐射部分的热烟道气间接接触。这可以通过，作为非限定性的实例，使原料通过位于炉子1的对流部分3内的换热管17来实现。被预热的原料的温度为200至600℉(95至315℃)。优选地，被加热的原料的温度为约300至500℉(150至260℃)，更优选地，温度为350至500℉(175至260℃)。
被预热的烃原料在41离开对流部分后，向其中加入水5和稀释蒸汽6形成混合物。水以加入的水和稀释蒸汽总重量的至少约1％至100％的量被加入到预热的原料中。优选地，水的加入量为水和稀释蒸汽重量的至少约3％(即约3％至约100％)。更优选地，水的加入量为水和稀释蒸汽重量的至少约10％，最优选至少约30％。应当理解，根据本发明的一个实施方案，烃原料中可以加入100％水，因此不加入稀释蒸汽。水流和稀释蒸汽流的总量构成达到希望的烃分压所要求的整个反应区H2O量。
如图1所示，水5优选在加入稀释蒸汽之前加入到预热的原料41中。据信，这种加入顺序将降低由于混合烃、水和稀释蒸汽造成的工艺流中不希望的压力波动。这种波动通常被称为水锤或汽锤。尽管向预热的烃原料中加入水和稀释蒸汽可以通过任何已知的混合设备完成，但是优选使用图中所示的喷雾器组合装置7。水优选在第一喷雾器8中加入。如图所示，第一喷雾器8包括被外导管10环绕的内部多孔导管9，以在内外导管之间形成环流空间11。优选地，预热的烃原料41流过环流空间11。还优选地，水5流过内部多孔导管9并通过内导管9的所示的开口(孔)注入预热的烃原料中。
稀释蒸汽6优选在第二喷雾器12中加入预热的烃原料中。如图所示，第二喷雾器12包括被外导管14环绕的内部多孔导管13，以在内外导管之间形成环流空间15。优选地，其中已加入水的预热的烃原料41流过环流空间15。还优选地，稀释蒸汽流过内部多孔导管13并通过内导管的所示的开口(孔)注入预热的烃原料中。
优选地，如图所示，所述第一和第二喷雾器是喷雾器组合装置的部件，其中所述喷雾器以流体流连通方式串联。如图所示，喷雾器8和12通过流体流互联器16以串联的流体流连通方式互相连通。
如附图中进一步图示说明的，在离开喷雾器组合装置7后，混合物(烃原料、水和稀释蒸汽)流回炉子1，在此该混合物在对流部分3的下部被进一步加热。所述烃原料的进一步加热可以采取本领域普通技术人员所知道的任意形式。然而，优选的是，加热包括使原料在炉子1的对流部分3的下部与来自炉子辐射部分的热烟道气间接接触。这可以通过，作为非限定性的实例，使原料通过位于炉子1的对流部分3内的换热管18完成。在18中再次加热混合物后，所得的被加热的混合物在19离开对流部分，然后流入炉子的辐射部分以进行烃的热裂化。流入辐射部分的被加热的原料的温度优选为800至1400℉(425至760℃)。优选地，被加热的原料的温度为约1050至1350℉(560至730℃)。
图1还描述了利用本发明控制进入辐射部分2的工艺温度。工艺温度是控制器26的输入量，所述控制器26控制水通过流量计28和控制阀29的流量。然后，水进入喷雾器7。当工艺温度太高时，控制器26增加水5的流量。
控制器26还向31图示的计算机控制装置发送流量信号，该计算机控制装置按照下面详述的方法确定稀释蒸汽的流量。通过流量计34测定烃原料33的预定流量，它是控制器35的输入量，控制器35又向原料控制阀36发送信号。控制器35还向计算机控制装置37发送原料流量信号，计算机控制装置37通过将原料流量乘以预定的总H2O与原料流量之比，确定加入辐射部分的总H2O。总H2O流量信号是计算机装置31的第二个输入量。计算机装置31从总H2O流量中减去所述水流量；该差值是稀释蒸汽控制器38的设定值。流量计39测试稀释蒸汽流量，该流量也是控制器38的输入量。当水流量增加时，如上所述，输入到稀释蒸汽控制器38的设定值降低。然后，控制器38命令控制阀40降低稀释蒸汽流量32至新的设定值。当工艺温度25太低时，控制系统命令控制阀29降低水的流量，并命令控制阀40增加蒸汽流量，同时保持恒定的总H2O流量。
或者，该控制系统以相同的方式工作，以如图2所示控制烟道气42的排放温度，和如图3所示控制炉子对流部分的工艺温度。关于对烟道气排出温度的控制，优选的是，烟道气在低于约650℉(345℃)，优选低于约450℉(230℃)，更优选低于约350℉(175℃)的温度下排出。
本发明的方法使得可以在炉子的辐射部分反应区中维持所需的烃分压，同时由于水流汽化的热量而更加满足了对流部分的热量回收要求。这种系统能够降低烟道气的排放温度，并因此提供更高能效的炉子。
类似地，本发明方法使得能够在设备中维持希望的反应区烃分压，所述设备中可以供给的稀释蒸汽是有限的和/或对于所希望的炉子操作条件而言是不足的。

Claims (12)

1.在炉子中处理烃原料的方法，该炉子具有对流部分和辐射部分，该方法包括：(a)加热烃原料以提供加热的原料，(b)向加热的原料中首先加入水和然后加入稀释蒸汽，以形成混合物，(c)在所述炉子的对流部分加热所述混合物，以提供加热的混合物，和(d)将来自(c)的加热的混合物进料到炉子的辐射部分中，其中向所述加热的原料中首先加入水和然后加入蒸汽的步骤(b)降低了所述混合物内压力的波动，和(e)根据至少一个工艺变量的波动改变加入到原料中的水与蒸汽的比以维持至少一个所述工艺变量基本上恒定。
2.权利要求1的方法，其中水以至少约3％重量的量加入，基于水和稀释蒸汽的总量计。
3.权利要求1的方法，其中水以至少约10％重量的量加入，基于水和稀释蒸汽的总量计。
4.权利要求1的方法，其中水以至少约30％重量的量加入，基于水和稀释蒸汽的总量计。
5.权利要求1的方法，其中炉子还包括烟道气部分，和其中所述至少一个工艺变量选自离开对流部分的被加热的混合物的温度、烟道气的排放温度和在对流部分中的烟道气温度。
6.权利要求5的方法，其中所得的加热的混合物被进料到炉子的辐射部分，并且其中工艺变量是所得到的加热的混合物进入炉子辐射部分前的温度。
7.权利要求6的方法，其中在炉子的烟道气部分中的烟道气的排放温度低于345℃。
8.权利要求6的方法，其中在炉子的烟道气部分中的烟道气的排放温度低于约230℃。
9.权利要求6的方法，其中在炉子的烟道气部分中的烟道气的排放温度低于约175℃。
8.任一前述权利要求的方法，其中水在第一喷雾器中加入，并且其中稀释蒸汽在第二喷雾器中加入所述加热的原料中。
9.权利要求8的方法，其中第一和第二喷雾器是喷雾器组合装置的部件，在所述喷雾器组合装置中第一和第二喷雾器以流体流连通方式串联连接。
10.权利要求1-7中任一项的方法，其中炉子是蒸汽裂化炉。
CNB038156342A 2002-07-03 2003-06-27 用水替代物裂化烃原料的方法 Expired - Lifetime CN100494318C (zh)

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
US10/188,461 US7138047B2 (en) 2002-07-03 2002-07-03 Process for steam cracking heavy hydrocarbon feedstocks
US10/188,901 2002-07-03
US10/188,901 US7090765B2 (en) 2002-07-03 2002-07-03 Process for cracking hydrocarbon feed with water substitution
US10/189,618 US7097758B2 (en) 2002-07-03 2002-07-03 Converting mist flow to annular flow in thermal cracking application
US10/189,618 2002-07-03
US10/188,461 2002-07-03

Publications (2)

Publication Number Publication Date
CN1665908A CN1665908A (zh) 2005-09-07
CN100494318C true CN100494318C (zh) 2009-06-03

Family

ID=30119026

Family Applications (3)

Application Number Title Priority Date Filing Date
CN03815733A Expired - Lifetime CN100587030C (zh) 2002-07-03 2003-06-27 重质烃原料的蒸汽裂化方法
CNB03815806XA Expired - Lifetime CN1281715C (zh) 2002-07-03 2003-06-27 在热裂化应用中将雾流转换为环形流
CNB038156342A Expired - Lifetime CN100494318C (zh) 2002-07-03 2003-06-27 用水替代物裂化烃原料的方法

Family Applications Before (2)

Application Number Title Priority Date Filing Date
CN03815733A Expired - Lifetime CN100587030C (zh) 2002-07-03 2003-06-27 重质烃原料的蒸汽裂化方法
CNB03815806XA Expired - Lifetime CN1281715C (zh) 2002-07-03 2003-06-27 在热裂化应用中将雾流转换为环形流

Country Status (9)

Country Link
EP (3) EP1523534B1 (zh)
JP (3) JP5166674B2 (zh)
KR (2) KR100945121B1 (zh)
CN (3) CN100587030C (zh)
AT (1) ATE396244T1 (zh)
AU (3) AU2003247756A1 (zh)
CA (3) CA2490403C (zh)
SG (1) SG177003A1 (zh)
WO (3) WO2004005432A1 (zh)

Families Citing this family (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7097758B2 (en) 2002-07-03 2006-08-29 Exxonmobil Chemical Patents Inc. Converting mist flow to annular flow in thermal cracking application
US7090765B2 (en) 2002-07-03 2006-08-15 Exxonmobil Chemical Patents Inc. Process for cracking hydrocarbon feed with water substitution
US7138047B2 (en) 2002-07-03 2006-11-21 Exxonmobil Chemical Patents Inc. Process for steam cracking heavy hydrocarbon feedstocks
ATE552322T1 (de) 2004-03-22 2012-04-15 Exxonmobil Chem Patents Inc Verfahren zum steamcracken von schweren kohlenwasserstoff-einsatzstoffen
ATE428764T1 (de) * 2004-05-21 2009-05-15 Exxonmobil Chem Patents Inc Verfahren und vorrichtung zur steuerung der temperatur eines erhitzten einsatzstoffs für eine flashtrommel, deren überkopfprodukt einsatzstoff für das cracken liefert
US7311746B2 (en) 2004-05-21 2007-12-25 Exxonmobil Chemical Patents Inc. Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid
US7402237B2 (en) 2004-10-28 2008-07-22 Exxonmobil Chemical Patents Inc. Steam cracking of hydrocarbon feedstocks containing salt and/or particulate matter
US7408093B2 (en) 2004-07-14 2008-08-05 Exxonmobil Chemical Patents Inc. Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks
US7312371B2 (en) 2004-05-21 2007-12-25 Exxonmobil Chemical Patents Inc. Steam cracking of hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US7488459B2 (en) 2004-05-21 2009-02-10 Exxonmobil Chemical Patents Inc. Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking
US7297833B2 (en) 2004-05-21 2007-11-20 Exxonmobil Chemical Patents Inc. Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors
US7358413B2 (en) 2004-07-14 2008-04-15 Exxonmobil Chemical Patents Inc. Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks
US7481871B2 (en) 2004-12-10 2009-01-27 Exxonmobil Chemical Patents Inc. Vapor/liquid separation apparatus
US7351872B2 (en) 2004-05-21 2008-04-01 Exxonmobil Chemical Patents Inc. Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace
US7247765B2 (en) 2004-05-21 2007-07-24 Exxonmobil Chemical Patents Inc. Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel
WO2006037805A2 (en) * 2004-10-08 2006-04-13 Shell Internationale Research Maatschappij B.V. Process to prepare ethylene and/or propylene from a carbon containing feedstock
US8696888B2 (en) 2005-10-20 2014-04-15 Exxonmobil Chemical Patents Inc. Hydrocarbon resid processing
GB0625528D0 (en) 2006-12-21 2007-01-31 Exxonmobil Chem Patents Inc Oligomerisation of olefins
KR100931792B1 (ko) 2007-05-25 2009-12-11 주식회사 엘지화학 탄화수소 수증기 열분해용 촉매, 그의 제조방법 및 이를이용한 올레핀의 제조방법
ITMI20071209A1 (it) * 2007-06-15 2008-12-16 Eni Spa Processo per la purificazione di una corrente acquosa proveniente dalla reazione di fischer-tropsch
KR100999304B1 (ko) 2007-07-05 2010-12-08 주식회사 엘지화학 올레핀 제조용 탄화수소 열분해 방법
CN101796167B (zh) * 2007-08-21 2013-05-01 埃克森美孚化学专利公司 烃原料的蒸汽裂化方法和设备
US8882991B2 (en) 2009-08-21 2014-11-11 Exxonmobil Chemical Patents Inc. Process and apparatus for cracking high boiling point hydrocarbon feedstock
US9181146B2 (en) 2010-12-10 2015-11-10 Exxonmobil Chemical Patents Inc. Process for the production of xylenes and light olefins
SG190307A1 (en) 2010-12-10 2013-06-28 Exxonmobil Chem Patents Inc Method and apparatus for obtaining aromatics from diverse feedstock
US20130291555A1 (en) 2012-05-07 2013-11-07 Phononic Devices, Inc. Thermoelectric refrigeration system control scheme for high efficiency performance
US9181147B2 (en) 2012-05-07 2015-11-10 Exxonmobil Chemical Patents Inc. Process for the production of xylenes and light olefins
US8893513B2 (en) 2012-05-07 2014-11-25 Phononic Device, Inc. Thermoelectric heat exchanger component including protective heat spreading lid and optimal thermal interface resistance
CN103215071A (zh) * 2013-04-12 2013-07-24 大连理工大学 一种费托油催化提质方法
US10458683B2 (en) 2014-07-21 2019-10-29 Phononic, Inc. Systems and methods for mitigating heat rejection limitations of a thermoelectric module
US9593871B2 (en) 2014-07-21 2017-03-14 Phononic Devices, Inc. Systems and methods for operating a thermoelectric module to increase efficiency
CN109694730B (zh) * 2017-10-24 2022-01-04 中国石油化工股份有限公司 一种原油裂解制备低碳烯烃的方法及装置
CN114616311A (zh) * 2019-03-15 2022-06-10 鲁姆斯科技有限责任公司 用于烯烃生产的配置
CN112694908B (zh) * 2020-12-15 2022-03-25 浙江大学 一种石油烃高效裂解方法
FI20225536A1 (fi) * 2022-06-16 2023-12-17 Coolbrook Oy Koksin muodostumisen estäminen hiilivetyjen käsittelylaitteissa

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB998504A (en) * 1963-04-18 1965-07-14 Lummus Co Method for cracking hydrocarbons
US6179997B1 (en) * 1999-07-21 2001-01-30 Phillips Petroleum Company Atomizer system containing a perforated pipe sparger

Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1053751A (zh) * 1900-01-01
GB199766A (en) * 1922-02-27 1923-06-27 Richard Wright Hanna Process for the continuous production of low boiling point hydrocarbons from petroleum oils
US2091261A (en) * 1929-04-17 1937-08-31 Universal Oil Prod Co Process for hydrocarbon oil conversion
US1984569A (en) * 1932-03-12 1934-12-18 Alco Products Inc Vapor phase cracking process
US2158425A (en) * 1936-01-04 1939-05-16 Union Oil Co Vacuum steam distillation of heavy oils
NL6802193A (zh) * 1967-02-23 1968-08-26
ES348993A1 (es) * 1967-04-26 1969-04-01 Continental Oil Co Proceso para mejorar la calidad de un aceite hidrocarburo de baja calidad para negro de carbon.
US4264432A (en) * 1979-10-02 1981-04-28 Stone & Webster Engineering Corp. Pre-heat vaporization system
US4311580A (en) * 1979-11-01 1982-01-19 Engelhard Minerals & Chemicals Corporation Selective vaporization process and dynamic control thereof
US4543177A (en) * 1984-06-11 1985-09-24 Allied Corporation Production of light hydrocarbons by treatment of heavy hydrocarbons with water
US4854944A (en) * 1985-05-06 1989-08-08 Strong William H Method for gasifying toxic and hazardous waste oil
US4840725A (en) * 1987-06-19 1989-06-20 The Standard Oil Company Conversion of high boiling liquid organic materials to lower boiling materials
JPH0819420B2 (ja) * 1988-09-05 1996-02-28 三井石油化学工業株式会社 低品位原料の分解処理方法
US5190634A (en) * 1988-12-02 1993-03-02 Lummus Crest Inc. Inhibition of coke formation during vaporization of heavy hydrocarbons
US4940828A (en) * 1989-10-13 1990-07-10 The M. W. Kellogg Company Steam cracking feed gas saturation
US5096567A (en) * 1989-10-16 1992-03-17 The Standard Oil Company Heavy oil upgrading under dense fluid phase conditions utilizing emulsified feed stocks
US5120892A (en) * 1989-12-22 1992-06-09 Phillips Petroleum Company Method and apparatus for pyrolytically cracking hydrocarbons
FR2710070A1 (fr) * 1993-09-17 1995-03-24 Procedes Petroliers Petrochim Procédé et dispositif de vapocraquage d'une charge légère et d'une charge lourde.

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB998504A (en) * 1963-04-18 1965-07-14 Lummus Co Method for cracking hydrocarbons
US6179997B1 (en) * 1999-07-21 2001-01-30 Phillips Petroleum Company Atomizer system containing a perforated pipe sparger

Also Published As

Publication number Publication date
JP2005531683A (ja) 2005-10-20
KR20050016709A (ko) 2005-02-21
JP5166674B2 (ja) 2013-03-21
EP1639060B1 (en) 2008-05-21
AU2003281371A1 (en) 2004-01-23
JP2005531684A (ja) 2005-10-20
JP4387301B2 (ja) 2009-12-16
WO2004005433A1 (en) 2004-01-15
CA2490403C (en) 2011-06-07
SG177003A1 (en) 2012-01-30
CN1665908A (zh) 2005-09-07
EP1527151A1 (en) 2005-05-04
KR100945121B1 (ko) 2010-03-02
EP1523534B1 (en) 2017-07-19
CA2489876C (en) 2011-04-19
CA2490403A1 (en) 2004-01-15
KR100979027B1 (ko) 2010-08-30
WO2004005431A1 (en) 2004-01-15
JP4403071B2 (ja) 2010-01-20
AU2003247756A1 (en) 2004-01-23
AU2003247755A1 (en) 2004-01-23
WO2004005432A1 (en) 2004-01-15
CN1665910A (zh) 2005-09-07
CA2489888C (en) 2011-07-12
CN100587030C (zh) 2010-02-03
CA2489888A1 (en) 2004-01-15
EP1523534A1 (en) 2005-04-20
KR20050016708A (ko) 2005-02-21
EP1527151B1 (en) 2018-07-18
CN1281715C (zh) 2006-10-25
JP2006508198A (ja) 2006-03-09
EP1639060A1 (en) 2006-03-29
ATE396244T1 (de) 2008-06-15
CA2489876A1 (en) 2004-01-15
CN1665909A (zh) 2005-09-07

Similar Documents

Publication Publication Date Title
CN100494318C (zh) 用水替代物裂化烃原料的方法
US7090765B2 (en) Process for cracking hydrocarbon feed with water substitution
JP5229986B2 (ja) 重質炭化水素原料の水蒸気分解方法
US20040004022A1 (en) Process for steam cracking heavy hydrocarbon feedstocks
EP0146117A2 (en) Flexible feed pyrolysis process
EP0110433B1 (en) Process and apparatus for the production of olefins from both heavy and light hydrocarbons
JPH09505086A (ja) 軽質及び重質炭化水素原料の水蒸気分解法及び装置
CN102083944A (zh) 裂解烃原料的炉的在运转中脱焦的方法
US20080207974A1 (en) Process for Decoking a Furnace for Cracking a Hydrocarbon Feed
CN102227488A (zh) 重质烃原料料流的裂化方法
US10870803B2 (en) Method for upgrading a hydrocarbon feed
CN1009833B (zh) 可弹性进料的热解工艺
CN101920187B (zh) 一种裂解反应制备低碳烯烃的设备及方法
US4906442A (en) Process and apparatus for the production of olefins from both heavy and light hydrocarbons
US9181495B2 (en) Convection zone of a cracking furnace
CN210163383U (zh) 轻质烃类增湿配汽系统
KR20050016718A (ko) 물의 치환을 이용하여 탄화수소 공급원료를 분해시키는 방법
CN116064094A (zh) 一种原油蒸汽裂解生产烯烃的方法及系统
TW202342706A (zh) 用於烯烴生產之低二氧化碳排放及氫氣輸入裂解加熱器
CN116848220A (zh) 用于含高沸点组分的轻质进料的蒸汽裂解炉的优化
CN107418613A (zh) 延迟焦化方法及其用途
CN116064095A (zh) 一种裂解重质原料生产烯烃的方法及系统
JPH01143637A (ja) 炭化水素の予熱方法
GB2114148A (en) Hydrorefining and/hydrocracking heavy hydrocarbon feeds
CS238738B1 (cs) Způsob přívodu tepla pro tepelné štěpení uhlovodíků a zařízení pro prováděni tohoto způsobu

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
CX01 Expiry of patent term

Granted publication date: 20090603

CX01 Expiry of patent term