CN210915872U

CN210915872U - Dehydrogenation device for C3/C4 mixed alkane

Info

Publication number: CN210915872U
Application number: CN201921823330.5U
Authority: CN
Inventors: 李湘平; 丁书兵; 胡楠; 胡智超; 仪军; 韩东辉
Original assignee: SHANDONG DONGMING PETROLEUM & CHEMICAL GROUP CO LTD
Current assignee: SHANDONG DONGMING PETROLEUM & CHEMICAL GROUP CO LTD
Priority date: 2019-10-28
Filing date: 2019-10-28
Publication date: 2020-07-03
Anticipated expiration: 2029-10-28

Abstract

The utility model relates to a mix dehydrogenation equipment field, in particular to C3C 4 mixes alkane dehydrogenation device contains: a feedstock pretreatment unit for filtering a mixed alkane feedstock; the deisobutanizer is connected with the raw material pretreatment unit and used for dehydrogenation, and outlets of the deisobutanizer and a storage device for storing the propane raw material are connected in parallel with an inlet of the reactor used for dehydrogenation reaction; the reactor outlet is connected to a hydrogen purification device to obtain hydrogen for delivery to downstream equipment. The utility model has simple structure and novel and reasonable design, improves the mixing degree of raw materials through the pretreatment unit, and effectively ensures the stable operation of the equipment; the raw material sources are further widened, the adaptability of the device is improved, the yield of the high value-added product propylene is improved after dehydrogenation reaction of C3/C4, the indexes such as energy consumption and material consumption can reach or exceed the design indexes, the product quality can reach the corresponding industrial standard, and the method has a very strong application prospect.

Description

Dehydrogenation device for C3/C4 mixed alkane

Technical Field

The utility model relates to a mix dehydrogenation equipment field, in particular to mixed alkane dehydrogenation device of C3C 4.

Background

The refinery liquefied gas mainly comes from catalytic cracking, ethylene and other devices of a refinery, and mainly comprises propane, propylene, butane and butylene. With the development of the petrochemical industry, in recent years, the proportion of refinery liquefied gas used as chemical raw materials is rapidly increased, and the refinery liquefied gas is mainly used for producing synthetic plastics, synthetic rubber and synthetic fibers and producing products such as medicines and dyes at the downstream. The existing dehydrogenation reaction device has the defects of complex structure, high cost, low utilization rate, low raw material conversion rate and the like due to the adoption of imported equipment.

Disclosure of Invention

Therefore, the utility model provides a C3C 4 mixed alkane dehydrogenation device, simple structure, novel in design is reasonable, and dehydrogenation performance is good, and is with low costs.

According to the design scheme provided by the utility model, the C3/C4 mixed alkane dehydrogenation device comprises a raw material pretreatment unit for filtering the mixed alkane raw material; the deisobutanizer is connected with the raw material pretreatment unit and used for dehydrogenation, and outlets of the deisobutanizer and a storage device for storing the propane raw material are connected in parallel with an inlet of the reactor used for dehydrogenation reaction; the reactor outlet is connected to a hydrogen purification device to obtain hydrogen for delivery to downstream equipment.

As the utility model discloses mixed alkane dehydrogenation device of C3C 4, furtherly, the deisobutanizer still is connected with the etherification device one that is used for generating etherate, the storage equipment of storage methyl alcohol raw materials and the butene treatment facility that carries out butene separation isomerism to carbon four behind the ether from the factory off-site are connected respectively to the entrance point of etherification device one.

As the utility model discloses mixed alkane dehydrogenation device of C3C 4, further, butene treatment facility still is connected with raw materials pretreatment unit through the pipeline.

As the utility model discloses mixed alkane dehydrogenation device of C3C 4, furtherly, the reactor still is connected with the deisobutanizer return circuit, has set gradually fractionation equipment, two, deoxidization equipment and saturated hydrogenation equipment of etherifying device on the deisobutanizer return circuit between the two at the reactor.

As the utility model discloses mixed alkane dehydrogenation device of C3C 4, further, deisobutanizer lower part still is provided with the butane isomerization equipment that is used for n-butane isomerization reaction return circuit.

The utility model has the advantages that:

the utility model has simple structure and novel and reasonable design, improves the mixing degree of raw materials through the pretreatment unit, and effectively ensures the stable operation of the equipment; the raw material sources are further widened, the adaptability of the device is improved, the yield of the high value-added product propylene is improved after dehydrogenation reaction of C3/C4, the indexes such as energy consumption and material consumption can reach or exceed the design indexes, the product quality can reach the corresponding industrial standard, and the method has a very strong application prospect.

Description of the drawings:

FIG. 1 is a schematic view of an embodiment of an apparatus;

FIG. 2 is a second schematic diagram of the apparatus of the embodiment;

FIG. 3 is a third schematic diagram of the apparatus of the embodiment.

In the figure, the reference numeral 1 represents a reactor, the reference numeral 2 represents a fractionation device, the reference numeral 3 represents a second etherification device, the reference numeral 4 represents an oxygen removal device, the reference numeral 5 represents a saturated hydrogenation device, the reference numeral 6 represents a butane isomerization device, the reference numeral 7 represents a deisobutanizer, the reference numeral 8 represents a hydrogen purification device, the reference numeral 9 represents a butene purification device, the reference numeral 10 represents a raw material pretreatment unit, the reference numeral 11 represents a butene isomerization device, the reference numeral 12 represents a first etherification device, and the reference numeral 13 represents an etherification device.

The specific implementation mode is as follows:

the present invention will be described in further detail with reference to the accompanying drawings and technical solutions, and embodiments of the present invention will be described in detail by way of preferred examples, but the embodiments of the present invention are not limited thereto.

Propylene is second only to ethylene, and its downstream derivatives mainly include polypropylene and propylene oxide, acrylonitrile, acrylic acid, cumene/phenol/acetone, oxo alcohols, isopropanol and other organic raw materials. In the long run, the global propylene market supply will continue to be extremely tight for a long time in the future. Propylene is the most important olefin other than ethylene, and is used second to ethylene only. The largest downstream product is polypropylene (PP), which accounts for about 60% of the global propylene consumption, and propylene can be used for preparing acrylonitrile, isopropanol, phenol, acetone, butanol, octanol, acrylic acid and esters thereof, propylene oxide, propylene glycol, epichlorohydrin, synthetic glycerin and the like. The global increase in propylene demand has exceeded ethylene due to the rapidly increasing demand for propylene derivatives, and it is difficult for conventional propylene production processes to meet the increasing demand. The capacity growth of the propylene market in China lags behind, and the market gap still exists in a considerable period of time in the future. The embodiment of the utility model provides a C3/C4 mixed alkane dehydrogenation device is shown with reference to fig. 1, contains: a feedstock pretreatment unit for filtering a mixed alkane feedstock; the deisobutanizer is connected with the raw material pretreatment unit and used for dehydrogenation, and outlets of the deisobutanizer and a storage device for storing the propane raw material are connected in parallel with an inlet of the reactor used for dehydrogenation reaction; the reactor outlet is connected to a hydrogen purification device to obtain hydrogen for delivery to downstream equipment. The purpose of the raw material pretreatment is to remove basic nitride, organometallic compound, water from the raw material. The raw material mixing degree is improved through the pretreatment unit, and the stable operation of the equipment is effectively ensured.

As the utility model discloses mixed alkane dehydrogenation device of C3C 4, further, it is shown with reference to fig. 2, the deisobutanizer still is connected with the etherification device one that is used for generating etherate, the storage equipment of storage methyl alcohol raw materials and to coming from the heterogeneous butene treatment facility of butene separation of carbon four behind the off-plant ether are connected respectively to the entrance point of etherification device one. Further, the butene treatment equipment is also connected with the raw material pretreatment unit through a pipeline. The raw material source is widened, the adaptability of the device is improved, and the device has a very strong application prospect.

As the utility model discloses mixed alkane dehydrogenation device of C3C 4, further, it is shown with reference to fig. 3, the reactor still is connected with the deisobutanizer return circuit, has set gradually fractionation equipment, two, deoxidization equipment and saturated hydrogenation equipment of etherification device on the deisobutanizer return circuit between the two. After dehydrogenation reaction of C3/C4, the yield of the high value-added product propylene is improved, indexes such as energy consumption, material consumption and the like can reach or exceed design indexes, and the product quality can reach corresponding industrial standards.

Continuous regeneration is achieved by transferring a small amount of catalyst from the reactor to a dedicated regeneration facility, while transferring the regenerated catalyst to the reactor. By continuously removing the deactivated catalyst and replenishing the regenerated catalyst, the reactor can stably operate and realize the highest product yield. The fresh feed needs to be pretreated to remove impurities such as basic nitrogen compounds, metals and moisture which affect the performance of the catalyst. The fresh propane and the circulating propane enter the reactor after being pretreated. According to the composition of raw materials, the pretreated butane and circulating butane are mixed and enter ORU deoxygenation equipment and CSP saturated hydrogenation equipment, and then enter a deisobutanizer after oxygen-containing compounds and olefins are removed. The normal butane with higher concentration can be separated from the lower part of the tower, and after the normal butane isomerization reaction of butane isomerization equipment, the normal butane returns to the tower to separate isobutane, and the high-purity isobutane separated from the top of the tower also enters the reactor. Propane and isobutane feeds are subjected to heat exchange with reacted materials and mixed with hydrogen in a separation system. The mixed propane, butane and hydrogen from the separation system are heat exchanged with the hot reaction mass in a heat combined feed heat exchanger. The mixture may be reacted in three reactors with a continuous catalyst regeneration system. The reaction mass is cooled, compressed, passed to a chlorine treater and a reaction mass dryer to remove Hcl, H2S and water, and then passed to a separation section where the reaction mass is divided into recycle gas, dry gas and liquid products. Through experimental test, under the operating mode of 100% processing load, through the utility model discloses the device scheme, can promote C3's processing proportion, make the C3 processing proportion of mixing dehydrogenation device, improve 10% (improving to 33.23% by 30% of design value) than the design value, the output of high added value propylene promotes 10.75%, the output of high added value product propylene has been improved, and the energy consumption, index such as material consumption all reaches or is superior to the design index, product quality reaches corresponding standard, improve equipment's whole processing benefit, energy-conservation subtracts the consumption, the cost is dropped into, improve enterprise economic benefits, better suitability and market spreading value have.

The term "and/or" herein means that three relationships may exist. For example, a and/or B may represent: a exists alone, A and B exist simultaneously, and B exists alone. In addition, the character "/" herein generally indicates that the former and latter associated objects are in an "or" relationship.

Unless defined otherwise, technical or scientific terms used herein shall have the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs. The use of "first," "second," and similar terms in the description and claims of this application do not denote any order, quantity, or importance, but rather the terms are used to distinguish one element from another. Also, the use of the terms "a" or "an" and the like do not necessarily denote a limitation of quantity. The word "comprising" or "comprises", and the like, means that the element or item listed before the word covers the element or item listed after the word and its equivalents, but does not exclude other elements or items. The terms "connected" or "coupled" and the like are not restricted to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", and the like are used merely to indicate relative positional relationships, and when the absolute position of the object being described is changed, the relative positional relationships may also be changed accordingly.

Exemplary embodiments of the present invention have been described in detail with reference to the preferred embodiments, however, it will be understood by those skilled in the art that various changes and modifications may be made to the specific embodiments described above and various combinations of the technical features and structures proposed by the present invention may be made without departing from the concept of the present invention, and the scope of the present invention is defined by the appended claims. The foregoing description of specific exemplary embodiments of the invention is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain certain principles of the invention and its practical application to enable one skilled in the art to make and use various exemplary embodiments of the invention and various alternatives and modifications as are suited to the particular use contemplated. It is intended that the scope of the invention be defined by the claims and their equivalents.

Claims

1. A C3/C4 mixed alkane dehydrogenation device, comprising:

a feedstock pretreatment unit for filtering a mixed alkane feedstock;

the deisobutanizer is connected with the raw material pretreatment unit and used for dehydrogenation, and outlets of the deisobutanizer and a storage device for storing the propane raw material are connected in parallel with an inlet of the reactor used for dehydrogenation reaction;

the reactor outlet is connected to a hydrogen purification device to obtain hydrogen for delivery to downstream equipment.

2. The C3/C4 mixed alkane dehydrogenation device of claim 1, wherein the deisobutanizer is further connected with a first etherification device for generating an etherified product, and inlet ends of the first etherification device are respectively connected with a storage device for storing a methanol raw material and a butene treatment device for separating and isomerizing butene from post-ether C4 from outside the plant.

3. The C3/C4 mixed alkane dehydrogenation unit of claim 2, wherein the butene treatment apparatus is further connected to the feedstock pretreatment unit by a line.

4. The C3/C4 mixed alkane dehydrogenation device of claim 1, wherein the reactor is further connected with a deisobutanizer loop, and a fractionation device, an etherification device II, an oxygen removal device and a saturation hydrogenation device are sequentially arranged on the deisobutanizer loop between the reactor and the deisobutanizer.

5. The C3/C4 mixed alkane dehydrogenation unit of claim 1, wherein the lower part of the deisobutanizer is further provided with a butane isomerization device for a n-butane isomerization reaction loop.