TW201546258A - Method and apparatus for obtaining crude oil products - Google Patents

Abstract

A method for obtaining crude oil products is proposed in which a gaseous stream (d) is formed from a crude oil stream (b) by evaporation (2) and the gaseous stream (d) is at least partially subjected to a steam cracking process (1), a cracked gas stream (e) being produced in the steam cracking process (1) which is at least partially quenched with a liquid hydrocarbon stream (f), thereby forming a quenching effluent (g). It is provided that a fraction (f) of the crude oil stream (b) that remains liquid during the evaporation (2) of the crude oil stream (b) is used at least partly to form the liquid hydrocarbon stream (f) used for the quenching. The liquid hydrocarbon stream used for the quenching is low in or free from components that have been separated from the quenching effluent (g) or a stream formed from the quenching effluent (g) and the quenching effluent (g) is obtained by quenching with the liquid hydrocarbon stream (f) at a temperature in the range from 0 to 250 DEG C. The invention also relates to an apparatus (100) configured to carry out the method.

Description

Method and apparatus for obtaining crude oil products

The present invention relates to a method and apparatus for obtaining a crude oil product according to the preamble of the independent item.

In the conventional refinery procedure, the crude oil is first desalinate and subjected to fractional distillation (hereinafter referred to as atmospheric distillation) under normal pressure after heating. The so-called residual atmospheric residue undergoes vacuum distillation.

However, not all fractions obtained during atmospheric distillation and vacuum distillation can be utilized economically. Some of the compounds contained therein may thus be catalytically reacted, for example, and valorised in this manner. However, this is not always completely successful. Thermal reactions of crude oil components cracked by steam are also known.

The present invention addresses the problem of improving the corresponding procedures and equipment, and in particular, increasing the yield of high value crude oil products.

One aspect of the present invention provides a method for obtaining a crude product, wherein the gas stream (d) is formed from the crude oil stream (b) by evaporation, and the gas stream (d) is at least partially subjected to a steam cracking process. (1) wherein, in the steam cracking procedure (1), a cracked gas stream (e) is produced, the cracked gas stream (e) is at least partially quenched with a liquid hydrocarbon stream (f), and a quenched effluent is formed (g) characterized in that the fraction (f) which remains liquid during the evaporation (2) of the crude oil stream (b) is at least partially used to form a hydrocarbon stream (f) for quenching, wherein for quenching The liquid hydrocarbon stream (f) contains little or no components which have been separated from the quench effluent (g) or from the stream formed by the quench effluent (g), and the quench effluent (g) is It is obtained by quenching a liquid hydrocarbon stream (f) at a temperature ranging from 0 ° C to 250 ° C.

Another aspect of the present invention provides an apparatus (100) for obtaining a crude product, which is configured to form a gas stream (d) from a crude oil stream (b) by evaporation, and to at least partially a gas stream (d) The steam cracking process (1) is carried out, wherein a cracking gas stream (e) is generated in the steam cracking process (1), and a quenching device (4) is provided, the quenching device (4) being configured to at least partially crack The gas stream (e) is quenched with a liquid hydrocarbon stream (f) to form a quench effluent (g) characterized in that the apparatus provided is configured to at least partially use the evaporation of the crude oil stream (b) (2) The fraction (f) of the liquid crude stream (b) is maintained during the period to form a liquid hydrocarbon stream (f) for quenching, wherein the apparatus provided is configured such that the liquid hydrocarbon stream (f) used for quenching contains a small amount Or containing no components that have been separated from the quench effluent (g), or from the stream formed by the quench effluent (g), and wherein the means provided are configured such that the quench effluent (g) is It is obtained by quenching a liquid hydrocarbon stream (f) at a temperature ranging from 0 ° C to 250 ° C.

The disclosure of the invention

This problem is solved by a method and apparatus according to the characteristics of the individual items. The examples are the subject matter of each of the sub-items and the following description.

For technical details of the terms used and the methods used, reference is made to the relevant specialist literature (see, for example, Zimmermann, H. and Walzl, R. (Zimmermann, H. and Walzl, R.): Ethylene ), in: Ullmann's Encyclopedia of Industrial Chemistry; Weinheim: Wiley-VCH (Weinheim: Wiley-VCH), online publication 2007, DOI: 10.1002/14356007.a10_045.pub2; and Irion , WW and Neuwirth, OS (Irion, WW and Neuwirth, OS: Oil): Refining, in: Ullmann's Encyclopedia of Industrial Chemistry, Weinheim: Wiley-VCH, Online Publication 2000, DOI: 10.1002/14356007 .a18_051).

The steam cracking procedure is generally carried out using a tube reactor, the reaction tubes of the tubular reactor, so-called coils, which can be operated individually or collectively under the same or different conditions. A reaction tube or a group of reaction tubes operating under the same or comparable conditions and a tubular reactor as a whole that may also operate under uniform conditions are hereinafter referred to as "cracking furnaces". The cracking furnace in the terminology used herein is thus a building block for steam cracking in which the same or comparable reaction conditions are prevailed. The steam cracking unit can comprise one or more cracking furnaces.

A gas stream formed from an effluent from one or more cracking furnaces is represented herein by a cracked gas stream. The cracked gas stream (also known as cracker effluent in English) is typically cooled in a cracked gas cooler with cooling water in a first cooling step, for example, a linear cooler (English) Cooled in a Transfer Line Exchanger and then cooled by quenching in a second cooling step, i.e., mixed with a liquid hydrocarbon stream.

In the specialist literature, the first cooling step, i.e. cooling with cooling water, such as cracking gas in a cracked gas cooler, is sometimes referred to as quenching. However, in this first cooling step, only the cracked gas is indirectly cooled, rather than being mixed with the liquid hydrocarbon stream as in the second cooling step. The second cooling step can therefore also be referred to as oil quenching, for a clearer distinction. The stream formed by combining the pyrolysis gas stream with the liquid stream for quenching is referred to herein as the quench effluent. Advantages of the invention

The present invention provides a process for obtaining a crude product wherein the gas stream is formed from the crude oil stream by evaporation and the gas stream is at least partially subjected to a steam cracking process. In the steam cracking process, a cracked gas stream is produced. The corresponding program is known, for example, from US 2008/0221378 A1 and WO 2010/117401 A1.

Within the scope of the present invention, at least some of the gas stream formed during the evaporation of the crude oil may be fed to one or more cracking furnaces either by itself or in combination with one or more other streams, such as one or more recycle streams. in. If there are multiple cracking furnaces, these can also be supplied in different streams. As is well known, in each case, the charging of the cracking furnace occurs after the addition of steam.

The resulting cracked gas stream is at least partially quenched with a liquid hydrocarbon stream to form a quench effluent. The present invention contemplates that the liquid crude oil stream stream maintained during the evaporation of the crude oil stream is at least partially used to form a liquid hydrocarbon stream for quenching, and the liquid hydrocarbon stream for quenching is contained with little or no A component that is separated from the stream formed by quenching the effluent (g) or from the quenched effluent (g). Further, the quench effluent is obtained by quenching a liquid hydrocarbon stream at a temperature ranging from 0 °C to 250 °C.

In other words, within the scope of the present invention, the liquid hydrocarbon stream for quenching is not formed using a recycle stream, and it is not conventional to use a quenching circuit as is conventional. In the quenching line of the conventional method, for example, the so-called oil tower system has two portions which are arranged one above the other. Quench oil is added to the top of the lower portion. The cracked gas stream is fed to the lower portion of the lower portion of the countercurrent to the quench oil. The heavy compound contained in the cracked gas stream is dissolved or suspended in the quench oil while cooling the cracked gas stream. Quench oil having any compound dissolved or suspended therein is withdrawn from the oil sump, selectively treated, and fed back to the top of the lower portion of the oil column. In the upper part of the oil column, pyrolysis gasoline is added, which is separated in the subsequently quenched water and also partially recycled.

However, a disadvantage of conventional quench lines is the aging of the quench oil. As a result of frequent contact with the pyrolysis gas stream, the initially low viscosity compounds are polymerized and form soot and tar or other viscous high boiling compounds. The quench oil is therefore routinely replaced periodically and replaced with fresh quench oil. The used quench oil is almost worthless. Conversely, by virtue of the fact that the liquid hydrocarbon stream contains little or no components which have been separated from the quenched effluent or from the stream formed by the quenching effluent, the liquid hydrocarbon stream for quenching according to the invention is The non-cyclic compound contained is only contacted once with the pyrolysis gas stream without undergoing any aging process, or hardly undergoing any aging process. Because it is only contacted once, there is no aging reaction, and the corresponding compound can be delivered to the product fraction that can still be utilized economically.

The cracked gas stream typically exits the radiant zone of one or more cracking furnaces at a temperature of from 750 °C to 875 °C. The cracked gas stream should be cooled as quickly as possible to prevent further reaction of the formed compound, such as, for example, the formation of a polymer. If a linear cooler as mentioned above is used, these carry out a considerable portion of the cooling of the cracked gas stream. As mentioned in the article "Ethylene" in Ullmann's Industrial Chemistry, which was previously referred to, the pyrolysis gas stream conventionally enters the oil column at a temperature of about 230 ° C and leaves at a temperature of about 100 ° C. . Most of the heat is taken away by the quenching oil. When quenching with the corresponding conventional oil, the temperature of the cracking gas is thus lowered from the temperature value in the first temperature range to the temperature value in the second temperature range, and the temperature value in the second temperature range is lower than the first temperature range The temperature value is about 130 ° C. When the process is carried out without the use of a linear cooler, the temperature difference between the temperature values is significantly higher.

From US 2008/0221378 A1, the procedure for using the unvaporized fraction of the crude oil stream for the initial step of the cold cracked gas stream is conventionally known, and the cracked gas stream has been obtained by steam cracking the evaporated fraction of the crude oil stream. The initial step is cooled to cleave any components present in the unvaporized fraction but still capable of being cracked by the heat of the cracked gas stream. It is therefore the case that the unvaporized fraction is added to the cracked gas stream within the cold range of the initial step, while the cracked gas stream is still at a relatively high temperature, typically 760 ° C to 929 ° C. At the same time, the initial step of cooling only slightly reduces the temperature of the cracked gas stream, ie typically does not exceed 111 °C. Downstream of the initial step, the resulting stream is therefore still at a very high temperature, which makes it necessary to carry out further quenching before further processing takes place. In other words, therefore, in the procedure according to US 2008/0221378 A1, the pyrolysis gas temperature during the initial step cooling is lowered from the temperature value in the first temperature range to the temperature value in the second temperature range, and the temperature value in the second temperature range The temperature value below the first temperature range is at most 111 °C. The temperature in the second temperature range is at least 649 °C.

Conversely, as a result of the quenching of the liquid hydrocarbon stream according to the present invention, as already mentioned, the quench effluent is obtained at a temperature ranging from 0 °C to 250 °C. The temperature may particularly fall within a temperature range from 50 ° C to 200 ° C, or from 50 ° C to 150 ° C, i.e., at a temperature which is also obtained in a conventional oil column, and allows the quench effluent to be directly processed further. Advantageously, in this case, the cracked gas stream has been cooled by means of a line cooler to, for example, a temperature of 50 ° C to 200 ° C above the quenching effluent, for example 100, before quenching with a liquid hydrocarbon stream. A temperature of from °C to 150 °C, and, for example, corresponds to a typical inlet temperature of an oil column that enters a conventional procedure. In this particularly preferred embodiment, the invention makes it possible to dispense with the use of other quench oils, particularly oil lines. There is no reason to do so based on US 208/0221378 A1, as this document teaches that the cracked gas stream must have a high temperature in order to crack any compound present in the unvaporized fraction of the crude oil stream. However, simply quenching to a low temperature by means of this unvaporized fraction will stop the corresponding cracking reaction and it will not be possible to achieve a reasonable cracking yield. Therefore, it is important for the effluent in the initial step to be at high temperatures, and therefore further quenching in the form of oil lines is indispensable.

The quenching effluent in a conventional steam cracking process is in a so-called oil column when the quench effluent contains a significant amount of fine oil droplets from the liquid stream used for quenching and high boiling components (oil, tar, and the like) First flow out of these ingredients. Downstream of the oil column alone may be a corresponding stream supplied to a conventional separation stage to recover hydrocarbon products from the cracked gas.

The present invention is now based on the omission of this type of oil sump and further processing the idea of quenching the effluent in the same manner as, for example, conventional processing of crude oil. This is possible because the liquid fraction is maintained during the evaporation of the crude oil stream, or its corresponding proportion is quenched, resulting in the quenched effluent containing only the type of conventional crude oil stream that is also found in atmospheric distillation (heavier) )ingredient.

Contrary to conventional procedures in which a quench oil line is provided, the liquid hydrocarbon stream for quenching is used only once within the scope of the present invention. Therefore, the main advantage of the proposed method is that the quenching does not require an oil line, wherein the oil (i.e., the liquid hydrocarbon stream conventionally used for quenching) is usually very aging due to chemical reactions and is particularly viscous. Significantly increased, and thus lost many of its value. Within the scope of the present invention, this type of aging reaction is not meaningful for explaining the reason. Another advantage of omitting the oil line is that, for example, it is no longer necessary to use an expensive heat exchanger in the oil line to routinely recover heat from the cracked gas, and heat can be supplied directly to the other by quenching the effluent. unit. Heat can be used, for example, for (pre)heating the stream used in atmospheric distillation. The residual liquid fraction during evaporation of the crude oil stream can also be cooled prior to use and its heat can be transferred to other streams.

Thus, it is particularly advantageous within the scope of the present invention if at least some of the separated feed formed by the quenching effluent is used to separate the distillation stream from another crude oil stream to produce a distillation effluent. This distillation separation is initially advantageously carried out in a distillation column configured for atmospheric pressure fractionation, as used in conventional refinery equipment. After atmospheric distillation, it can be vacuum distilled in a distillation column configured for this purpose. All of the streams (cuts, fractions) formed during distillation (e.g., atmospheric distillation and/or vacuum distillation) are referred to herein as distillation effluents.

The separated feed may be formed from the quench effluent in any desired manner, but will always comprise hydrocarbons having one, two, three, four or more carbon atoms contained in the quench effluent and/or For example, hydrocarbons formed from such hydrocarbons by hydrogenation or further reaction after quenching. These may be, for example, methane, ethane, ethylene, acetylene, propane, propylene and propyne, and saturated hydrocarbons and unsaturated hydrocarbons having four carbon atoms. The "formation" of the separated feed as discussed may be carried out, for example, by separating a portion of the stream, combining it with another stream, or by chemical and/or physical reaction.

In addition, the separated feed advantageously comprises hydrocarbons previously present in the liquid hydrocarbon stream for quenching, or compounds formed from such hydrocarbons. These are typically hydrocarbons having more than 10 or 20 and for example up to 30 or more carbon atoms. This type of hydrocarbon thus advantageously does not require separation from the quench effluent, but according to an advantageous embodiment of the procedure, more particularly unchanged, undergoes joint distillation separation with the second crude oil stream.

In other words, an embodiment is proposed in which the combined distillation of the quenched effluent undergoes separation with the second crude oil stream. In this manner, as explained below, full integration into the refinery is achieved, such as by atmospheric distillation of the entire quench effluent with the second crude stream fed to a suitably configured distillation column. This enables a separate separation device for the hydrocarbons in the steam cracking stream or quenching effluent. For example, the quench effluent can be delivered with a liquid hydrocarbon stream for quenching to a corresponding distillation column in which a conventional crude oil fraction is obtained. The compounds contained in the liquid hydrocarbon stream for quenching form respective fractions based on their boiling points, such as vacuum gas oil or atmospheric gas oil. It is therefore not necessary to use any conventional oil column apparatus to further separate any of the compounds contained in the liquid hydrocarbon stream for quenching. When pyrolysis gasoline also produces a corresponding fraction of crude oil distillation, ie, a gasoline fraction, water quenching may also be omitted. There is also no need to separately compact the quench effluent.

The procedure can therefore be achieved with significantly less expenditure equipment than according to prior art procedures, as exemplified in US 2009/0050523 A1, which only feeds the heavy fraction separated from the cracked gas in a conventional manner into the refinery process. . Starting from US 2009/0050523 A1, the procedure according to the invention is not obvious, since the quenching oil and pyrolysis gasoline lines used in US 2009/0050523 A1 require the separation of quench oil from pyrolysis gasoline. It is therefore not possible to deliver the corresponding compound in the quench effluent for combined separation with the second crude oil stream. The same is true for the program as exemplified in US 2007/0055087 A1. US 2010/0320119 A1 discloses a procedure in which the quench effluent undergoes a primary fractionation resulting in a different stream. However, because US 2010/0320119 A1 explicitly teaches the preparation of a tar stream from primary fractionation and its use in a quench oil line, it is not possible to feed the second crude stream to the primary fractionation as this will result in the recovery of the tar stream. It became impossible because of the feed of other crude oil components.

In other words, in an advantageous embodiment, the invention proposes to initially treat a separated feed using a quench effluent, such as a conventional crude oil stream, by atmospheric distillation. In atmospheric distillation, the products of the steam cracking process, such as ethylene and other light hydrocarbons, form the overhead stream of the distillation column. At the same time, a conventional fraction of the crude oil stream (and a liquid stream for quenching) can be produced in this distillation column.

Within the scope of this preferred embodiment of the invention, the oil column conventionally used in the steam cracking process and the distillation column used for atmospheric distillation in a conventional refinery process are thus functionally combined. If present, the steam cracking process product withdrawn from the top of the column or overhead of the column for atmospheric distillation can be subjected to a step generally after the oil column of the steam cracking process with the corresponding light product from the crude oil stream to produce a cracked gas.

For example, water washing can be used initially, in which any petroleum brain (naphtha) still contained in the corresponding stream is precipitated in liquid form. After washing with water, hydrocarbons usually having one to four carbon atoms remain in the gas phase. These can then be subjected to conventional separation sequences (first Demethanizer, first Deethanizer, etc.; for details, reference is made to the cited professional literature).

The further distillation effluent produced in the atmospheric distillation column is composed of heavier hydrocarbons, the heavier hydrocarbons being primarily derived from uncracked crude oil or liquid streams for quenching. These may be, for example, so-called atmospheric gas oil (AGO) and the atmospheric residue previously mentioned.

Other advantages are obtained if certain hydrocarbons, such as those contained in the cracked gas or other crude oil streams, undergo another steam cracking procedure. This type of stream that undergoes a steam cracking procedure again is referred to as a recycle stream. The recycle stream is selectively combined with the fresh feed and together, or separately from each other, fed to the same or different cracking furnace. The fresh feed used within the scope of the present invention is a gas stream formed during the evaporation of the crude oil stream, as explained above, but other streams supplied from the battery limit may also be used.

Separation of the fraction provided as a recycle stream can be carried out in the same manner as conventional steam cracking procedures, for example, in a conventional separator provided within the scope of the present invention. Therefore, different separations for the corresponding light components, as conventionally occurring in refinery, are not required. This type of volatile component does not need to be stored in a tank as in conventional refinery equipment because it can be fed to the steam cracking process as a recycle stream. As also explained below, the compounds contained in the corresponding streams can also be at least partially further reacted.

Overall, the measure according to the invention has the advantage that no oil column is required and pyrolysis oil and pyrolysis gasoline as separate products are not obtained. When the procedure according to the invention is used, compounds which conventionally produce pyrolysis oil and pyrolysis gasoline are found in the corresponding distillation effluent (for example from atmospheric distillation and vacuum distillation).

By recycling all of the distillation effluent that is not intended as a product, the process according to the invention can also be configured such that typical refinery products such as gasoline, diesel, fuel oil and the like are no longer produced. The above ingredients, for example, after suitable treatment, such as hydrotreating or (mild) hydrocracking, together or separately, can be used as starting materials for the steam cracking procedure. In such cases, for example, only ethylene, propylene, butadiene, aromatics, and pressurized steam or electricity can be obtained from the added crude oil. This change proves that the system is very economical. The program according to the invention can be flexibly adapted to the specific requirements of the various compounds.

The invention also makes it possible to utilize the waste heat generated in the steam cracking process particularly efficiently. This heat can first be used to preheat the crude oil stream, and the vaporized portion is then subjected to a steam cracking procedure. Other waste heat can be used, for example, to heat other crude oil streams that are subsequently fed to a distillation column for atmospheric distillation. Overall, this leads to favorable energy integration and reduced waste heat that must be removed. The crack gas cooler can also be integrated into a corresponding heat recovery line, such as using steam generated therein to heat the crude oil stream.

The distillation separation of the separated feed formed using the quench effluent with other crude oil streams is advantageously carried out, as explained, starting at atmospheric pressure and then under vacuum, so that distillation can be used with refinery technology. Conventional methods are employed, and corresponding methods of treating the distillation effluent can also be used.

As already mentioned, the distillation effluent or stream thus derived also at least partially undergoes a steam cracking procedure. The secondary stream can be formed, for example, by bridging a partial stream, combining with other streams, chemically or physically reacting at least some of the components in the corresponding stream, heating, cooling, evaporating, condensing, and the like.

It is particularly advantageous that the corresponding secondary stream can be formed by a hydrocracking procedure. In these procedures, the distillation effluent is selectively or fully catalytically hydrogenated and at least partially cleavage, optionally after further separation and/or preparation. In this manner, unsaturated hydrocarbons that are not intended to be fed to the furnace can be converted to saturated hydrocarbons and reacted again in a steam cracking procedure to form high value products.

The recycle stream can be, in particular, atmospheric gas oil (AGO) treated by hydrotreating and/or hydrocracking and vacuum gas oil (VGO) treated by hydrotreating and/or hydrocracking, ie , distillation residue from atmospheric distillation or vacuum distillation. Other recycle streams may comprise unsaturated hydrocarbons having two to four carbon atoms and/or hydrocarbons having five to eight carbon atoms. The petroleum brain can also be used again in the corresponding steam cracking procedure.

In the separation step in which a hydrocarbon having two to four carbon atoms is carried out after distillation separation, a compound such as methane, ethylene, propylene, butadiene and/or an aromatic compound (benzene, toluene) can be obtained. And / or xylene, collectively known as BTX), and removed from the device. Combustion can be produced during vacuum distillation and there is no vacuum residue for further use and/or methane formed can be burned to recover energy.

An apparatus for producing a crude oil product is also the subject of the present invention configured to form a gas stream from a crude oil stream by evaporation and subject the gas stream to at least partially undergo a steam cracking procedure. The apparatus is configured to generate a cracked gas stream in a steam cracking process, the cracked gas stream being at least partially quenched by the liquid hydrocarbon stream to produce a quench effluent. In accordance with the present invention, an apparatus is provided that is configured to at least partially use a crude oil stream fraction that maintains a liquid state during evaporation of a crude oil stream to form a liquid hydrocarbon stream for quenching. The liquid hydrocarbon stream for quenching contains little or no ingredients that have been separated from the stream formed by the quench effluent or from the quench effluent. In addition, the quench effluent is obtained by quenching a liquid hydrocarbon stream at a temperature in the range of 0 °C to 250 °C.

This type of device contains all the devices that enable it to carry out the program according to the invention. Advantageously, the apparatus according to the invention comprises at least one distillation column configured for atmospheric pressure fractionation; and apparatus configured to supply a separated feed formed using at least a portion of the quenched effluent and another crude oil stream to the distillation column .

Advantageously, an apparatus is also provided which is likewise configured to at least partially undergo a steam cracking procedure for the distillation effluent formed in this distillation column, or the stream derived therefrom.

The invention is explained in more detail with reference to the drawings showing preferred embodiments of the invention.

Figure 1 schematically illustrates a partial view of an apparatus for producing a crude product, generally designated 100, in accordance with one embodiment of the present invention.

The crude oil supplied to the equipment 100 is divided into two crude oil streams b and a crude oil stream c. The crude oil stream b is preheated in the convection zone of one or more cracking furnaces 1 and sent to the evaporation vessel 2. A portion of the crude oil stream b evaporated in the evaporation vessel 2, after being mixed with the stream, passes through the radiation zone of the one or more cracking furnaces 1 as a stream d, and a cracking gas e is obtained.

The cracked gas e is cooled in the cracked gas cooler 3 and then quenched in a quenching unit 4 using a portion of the crude oil stream b depicted in stream f, which is maintained in a liquid state in the evaporation vessel 2. A separated feed (not specifically shown) formed from the quench effluent g is sent to a distillation column 5 for fractionating atmospheric distillation in which the crude oil stream c is also fed.

The distillation column 5 is operated in a conventional manner to, for example, obtain a normal pressure residue h and a normal pressure gas oil i therein. From the top of the distillation column 5 or from the upper portion of the distillation column 5, a stream k containing light products from one or more cracking furnaces 1 and a crude oil stream c is withdrawn. The water-petroleum mixture is precipitated from stream k by a water mix (not shown) in a water washer 6, and is sent as stream l to a decanter 7. In this decanter, a water stream m and a petroleum brain stream n are obtained.

The fraction remaining in the form of a gas in the water scrubber 6 is withdrawn as stream o and fed to a fractionation section which may be of conventional configuration, the fraction being substantially a hydrocarbon having one to four carbon atoms. In the corresponding fractionation section, for example, methane and/or methane and ethane may first be separated (so-called first demethanizer or first deethanizer procedure).

FIG. 2 shows an enlarged view of device 100, ie, as an enlarged detail of complete device 100, generally indicated at 200. The part of the apparatus shown in Figure 1 is denoted as 100, i.e., at least one cracking furnace 1 and associated apparatus 2 to 4 and a distillation column 5 configured for fractional atmospheric distillation, with a water scrubber 6 and associated decantation 7.

As shown in Fig. 2, the vacuum residue p is obtained from the atmospheric residue which is extracted from the distillation column 5 as h in the distillation column 8 which is arranged for vacuum distillation; this vacuum residue p can be in the device 9. Burned and used to recover energy as indicated by arrow q.

The overhead stream r from the distillation column 8, so-called vacuum gas oil, is sent to a hydrogenation reaction unit 10 in which the stream r can be processed by, for example, hydrocracking. The corresponding process stream s can be recycled to the steam cracking process or to one or more cracking furnaces 1. The same applies to the above-mentioned stream i, atmospheric gas oil, which can be treated in the hydrogenation reaction unit 11 and then recycled as a stream t to the steam cracking process. From a stream u consisting essentially of a hydrocarbon having five to eight carbon atoms, the aromatic compound can be separated in the aromatic extraction unit 12 and discharged from the apparatus as stream v. The residual fraction can be subjected to another steam cracking procedure as stream w. The previously described stream comprising predominantly hydrocarbons having from one to four carbon atoms can be delivered to the C4 fractionation section 13, wherein, for example, a product stream, such as ethylene, generally referred to herein as x can be isolated. , propylene and butadiene. The methane stream y can be discharged from the apparatus and/or used for heating. Hydrocarbons not obtained as product stream x can be recycled to the steam cracking process as stream z.

1‧‧‧ cracking furnace
2‧‧‧Evaporation container
3‧‧‧Cleavage gas cooler
4‧‧‧Quenching device
5, 8‧‧‧ distillation tower
6‧‧‧Washer
7‧‧‧ Decanter
9‧‧‧ device
10, 11‧‧‧ Hydrogenation unit
12‧‧‧Aromatic extraction unit
13‧‧‧C4 fractionation section
100, 200‧‧‧ equipment
b, c‧‧‧ crude oil flow
d, f, k, l, o, s, t, u, v, w, z‧‧ ‧ flow
e‧‧‧Cleavage gas
g‧‧‧Quench effluent
h‧‧‧Atmospheric residue
i‧‧‧Normal pressure gas oil
m‧‧‧Water flow
n‧‧‧Petroleum
P‧‧‧vacuum residue
Q‧‧‧ arrow
R‧‧‧top flow
x‧‧‧Product stream
Y‧‧‧methane flow

Figure 1 shows a partial view of an apparatus for recovering crude oil products in accordance with one embodiment of the present invention.

Figure 2 shows an enlarged view of an apparatus for recovering crude oil products in accordance with one embodiment of the present invention.

In the drawings, the same reference numerals are given to the elements corresponding to each other, and the repeated description is omitted. The components of the device are shown synchronously with respect to the steps of the program.

1‧‧‧ cracking furnace

2‧‧‧Evaporation container

3‧‧‧Cleavage gas cooler

4‧‧‧Quenching device

5‧‧‧Distillation tower

6‧‧‧Washer

7‧‧‧ Decanter

100‧‧‧ Equipment

b, c‧‧‧ crude oil flow

d, f, k, l, o‧‧‧ flow

e‧‧‧Cleavage gas

g‧‧‧Quench effluent

h‧‧‧Atmospheric residue

i‧‧‧Normal pressure gas oil

m‧‧‧Water flow

n‧‧‧Petroleum

Claims (11)

A method for obtaining a crude product, wherein a gas stream (d) is formed from a crude oil stream (b) by evaporation, and the gas stream (d) is at least partially subjected to a steam cracking process (1) Wherein, in the steam cracking procedure (1), a cracked gas stream (e) is produced, the cracked gas stream (e) is at least partially quenched with a liquid hydrocarbon stream (f), and a quench is formed An effluent (g) characterized in that a fraction (f) which remains liquid during the evaporation (2) of the crude oil stream (b) is at least partially used to form the hydrocarbon stream (f) for quenching, wherein The hydrocarbon stream (f) for quenching the liquid phase contains little or no components which have been separated from the quenched effluent (g) or from the stream formed in the quench effluent (g), and The quench effluent (g) is obtained by quenching the liquid hydrocarbon stream (f) at a temperature ranging from 0 °C to 250 °C. The method of claim 1, wherein a separate feed is formed from at least a portion of the quench effluent (g) and is separated from the further crude oil stream (c) by distillation ( 5, 8) to form a distillation effluent (h, i, k, p, r). The method of claim 2, wherein the distillation effluent (h, i, k, p, r) or first-class (s, t, w, z) derived therefrom is at least partially used as a recycle stream. The steam cracking procedure (1) was carried out. The method of claim 2, wherein the distillation separation (5, 8) of the separated feed together with the further crude oil stream (c) is initially carried out at atmospheric pressure (5), And then carried out under vacuum (8). The method of claim 3, wherein the stream (s, t) derived from at least a catalytic hydrogenation reaction (10, 11) is from at least a portion of the distillation effluent (i, r) Formed in ). The method of any one of claims 3 to 5, wherein the atmospheric gas oil (i) is treated by the catalytic hydrogenation reaction (11), and the vacuum gas oil (r) is Treated by the catalytic hydrogenation reaction, a saturated hydrocarbon having two to four carbon atoms (z) and/or a hydrocarbon having five to eight carbon atoms (w) is used as a recycle stream. The method of any one of claims 2 to 6, wherein methane, ethylene, propylene and/or butadiene (x) and/or aromatic compound (v) are obtained. The method of any one of claims 2 to 7, wherein at least a portion of the distillation effluent (p, y) is combusted to recover energy. An apparatus (100) for obtaining a crude product, configured to form a gas stream (d) from a crude oil stream (b) by evaporation, and at least partially perform a steam cracking of the gas stream (d) a program (1), wherein a pyrolysis gas stream (e) is produced in the steam cracking process (1), and a quenching device (4) is provided, the quenching device (4) being configured to at least partially The pyrolysis gas stream (e) is quenched with a liquid hydrocarbon stream (f) to form a quench effluent (g) characterized in that the apparatus provided is configured to at least partially use the evaporation of the crude oil stream (b) (2) maintaining a liquid fraction (f) of the crude oil stream (b) during the period to form the liquid hydrocarbon stream (f) for quenching, wherein the apparatus provided is configured to cause the liquid to be quenched The hydrocarbon stream (f) contains little or no components that have been separated from the quench effluent (g), or from the stream formed by the quench effluent (g), and wherein the means provided are configured such that The quench effluent (g) is obtained by quenching the liquid hydrocarbon stream (f) at a temperature ranging from 0 °C to 250 °C. The apparatus (100) of claim 9, comprising the apparatus (100) configured to perform the method according to any one of claims 1 to 8. The apparatus (100) of claim 9 or 10, comprising at least one distillation column (5, 8) configured for fractionation, the apparatus provided being configured to use the quench effluent ( g) forming a separate feed and supplying the separated feed and a further crude oil stream (c) to the at least one distillation column (5, 8).