CN215480733U

CN215480733U - Membrane type fixed bed catalyst crude gas waste heat recovery and hydrogen utilization riser

Info

Publication number: CN215480733U
Application number: CN202120023503.6U
Authority: CN
Inventors: 张国杰; 葛霖; 葛京鹏; 葛亮
Original assignee: Yangzhou Youwei Energy Saving Technology Co ltd
Current assignee: Ge Lin
Priority date: 2021-01-06
Filing date: 2021-01-06
Publication date: 2022-01-11
Anticipated expiration: 2031-01-06

Abstract

The utility model discloses a membrane type fixed bed catalyst crude gas waste heat recovery and hydrogen utilization ascending pipe, which comprises a shell of the ascending pipe and a bridge pipe tee joint, wherein a crude gas channel is arranged in the ascending pipe; the inner layer of the pipe wall of the shell of the ascending pipe is a pipe wall heat-insulating layer, a temperature control and waste heat recovery device is arranged in the inner circle of the pipe wall heat-insulating layer, and a working medium for taking away waste heat of raw coke oven gas is introduced into the temperature control and waste heat recovery device; and an anticorrosive ceramic layer is attached to the surface of the outer layer of the temperature control and waste heat recovery device, or a mixed layer combining the anticorrosive ceramic layer and the membrane type fixed bed catalyst layer is attached to the surface of the outer layer of the temperature control and waste heat recovery device. The utility model enables the hydrogen-rich raw coke oven gas to generate directional reaction under the action of a proper temperature and a catalyst, eliminates the technical bottleneck problem of the existing coke oven production process, simultaneously improves the reliability and the stability of the riser, and is beneficial to the long-term stable and safe operation of the system.

Description

Membrane type fixed bed catalyst crude gas waste heat recovery and hydrogen utilization riser

Technical Field

The utility model relates to the field of coal coke ovens, in particular to a coke oven energy-saving and gas hydrogen resource utilization device thereof, which is particularly suitable for the coke oven coking process to synthesize membrane type fixed bed catalyst crude gas waste heat recovery and hydrogen utilization ascending pipes by means of crude gas hydrogen enrichment in different coking periods.

Background

In the coking process, coking coal is heated and dry distilled in a coke oven in an air-isolated way to generate coke, and simultaneously, a large amount of raw coke gas is generated, the coke oven is usually formed by a plurality of carbonization chambers (hearths) in parallel, each carbonization chamber is provided with a raw coke gas riser outlet, the coal is dried to obtain high-temperature raw coke gas with the temperature of about 850 ℃ in the coking process in the carbonization chamber with the temperature of 1000 +/-50 ℃, and the raw coke gas enters a riser assembly through the raw coke gas outlet of the carbonization chamber and enters a gas collecting pipe after being subjected to ammonia water temperature reduction. In the coking process, distillate of the crude gas is different at different time in the coking process, the distilled crude gas in the early coking stage mainly contains macromolecular coal tar, the distilled crude gas in the later coking stage mainly contains light micromolecule gas, the light micromolecule gas in the later coking stage mainly comprises H2 and CH4, wherein H2 accounts for 40-60%. At present, hydrogen in the coal gas is basically prepared into coal gas and burnt as fuel, and the hydrogen is an important chemical resource and can be used as hydrogenation reaction raw material for lightening macromolecular coal tar. The gas generated in the later stage of the coking process is rich in hydrogen, and has high chemical activity due to high temperature. The coke oven needs to control the temperature of raw gas in the space at the top of the coking chamber (furnace top space temperature control), according to the regulation of coke oven technical management regulations, the temperature of the furnace top space is preferably controlled to be 800 +/-50 ℃, is not more than 850 ℃, and is too high, so that the coke oven gas is subjected to secondary cracking at the top of the coking chamber, a large amount of deposited carbon is attached to the top of the coking chamber, and the space temperature is too high, which can cause unqualified quality of chemical recovery tar, such as increased specific gravity, increased viscosity and difficult dehydration of the tar. Opening the riser covers (at most, not more than three) 10-20 minutes ahead of the coke pushing plan, closing the bridge pipe water seal flap valve, opening the dust removal hole cover far away from the riser, sucking air, and burning off graphite at the top of the carbonization chamber. In coke oven production, the common methods for eliminating graphite are: the graphite is swept by compressed air, the graphite is swept by an empty furnace, and the graphite is swept by a scraper arranged at the top of a coke pushing head.

The byproduct of the coal tar coking production process is a complex mixture with ten thousand components, and about 500 more single compounds which are separated and identified at present account for about 55 percent of the total amount of the coal tar, wherein the single compounds comprise 174 neutral components such as benzene, dimethylbenzene, naphthalene and the like; phenol, cresol, etc. 63 kinds of acid component and 113 kinds of alkali component. Although some components have high value, the content of the components in coal tar is very small, and only 13 varieties account for more than l percent, and the varieties are naphthalene, phenanthrene, fluoranthene, fluorene, anthracene, pyrene (melting point is 150 ℃), acenaphthene, carbazole, 2-methylnaphthalene, 1-methylnaphthalene, dibenzofuran and cresol. Many compounds in the coal tar are plastics, synthetic rubber, pesticides, medicines, high-temperature resistant materials and valuable raw materials in the national defense industry, and a part of polycyclic hydrocarbon compounds cannot be produced and replaced by the petrochemical industry. Coal tar is mainly used for processing and producing light oil, phenol oil, naphthalene oil, modified asphalt and the like, and then is further processed to prepare various chemical raw materials such as benzene, phenol, naphthalene, anthracene and the like, although the product quantity is large and the application is wide, the product quantity is less than that of more than 500 compounds in the coal tar. The coal tar after simple processing has low utilization value, and the application of the deep processing refined product is generally seen at home and abroad. The processing technology of coal tar at home and abroad is largely the same and different, and is dehydration and fractionation, and the main research direction of coal tar processing is to increase product varieties, improve product quality grade, save energy and protect environment.

The coal tar hydrogenation refinement has the functions of desulfurization, denitrification, deoxidation and hydrogenation saturation, part of unsaturated olefin and aromatic hydrocarbon bonds in the coal tar are saturated in the hydrogenation process, and the desulfurization, denitrification and deoxidation rates of the coal tar in the section respectively reach more than 96%, 85% and 97%, so that the requirements of cracking raw materials are met. The hydrogen/carbon ratio of the product is increased from 1.11 of the raw oil to 1.58, so that the coal tar is partially lightened in the working section. The hydrocracking section further removes hetero atoms such as sulfur, nitrogen, oxygen and the like in the raw oil, the products are further lightened, and most of the raw material is hydrocracked to generate light fractions such as gasoline, diesel oil and the like. After the cracking section, the removal rate of the heteroatoms can reach over 99.5 percent, and the hydrogen/carbon ratio can reach 1.62. After the coal tar is subjected to three-stage hydrogenation, the product oil is lighter and cleaner, and high-value naphtha distillate oil and diesel distillate oil can be obtained after rectification.

The hydrogenation of coal tar increases with the conversion rate of heavy oil of the coal tar, the hydrogen consumption increases slowly after increasing rapidly, the oil yield is similar to the hydrogen consumption and increases finally, and the gas yield is in an increasing trend. The hydrogen is a reactant of the hydrocracking reaction of the tar heavy oil, and the oil yield and the gas yield are concurrent products of the hydrocracking reaction of the tar heavy oil. As the reaction temperature and the reaction time increase, the hydrogenation reaction depth of the tar heavy oil increases, and hydrogen gas participating in the reaction increases, so that the hydrogen consumption increases. In the initial stage of the tar heavy oil reaction, a large number of condensed ring cracking intermediate products need to be hydrogenated stably, so that the hydrogen consumption in the initial stage is increased rapidly along with the increase of the reaction depth; in the later reaction stage, most of condensed ring organic matters which are difficult to crack are cracked, and oil products of monocyclic or bicyclic molecules with fewer rings are generated. Although the monocyclic aromatic hydrocarbon is difficult to be hydrocracked in the later period, branched chains on the aromatic ring type compound can undergo further cracking reaction at high temperature to generate organic matters with smaller molecular size, and the cracking rate of the organic matters to obtain the small molecular gas is higher, so that the later generation rate of the gas yield is higher. Because a large amount of polycyclic aromatic hydrocarbon unsaturated hydrogenation is carried out in the early stage, the hydrogen consumption in the later stage is reduced, which shows that the hydrogen consumption in the later stage of the reaction tends to be slowly increased. The change rule of hydrogen consumption and oil yield reflects the rule of the parallel reaction of the hydrocracking reaction of the tar heavy oil. After the fused ring substances are subjected to dehydrogenation, ring opening and dealkylation and decomposed into oil product molecules with smaller molecular weight, the cracking of the fused ring macromolecules is reduced. Meanwhile, the number of small molecule oils increases, the hydrocracking rate increases, and thus the oil yield selectivity goes down. Similarly, the yield selectivity of the generated gas is continuously increased along with the increase of the conversion rate, because the gas amount generated by cracking the micromolecule oil is increased along with the increase of the reaction conversion rate, and the gas yield is increased. From the change rule of the oil yield selectivity and the gas yield selectivity in the later stage of the conversion rate, it can be seen that the proper selection temperature, time and the like are very important for controlling the selectivity of oil products in the catalytic hydrocracking process of the heavy tar oil. Namely, the reaction time and the reaction temperature under the low-temperature reaction condition are the decisive factors influencing the denitrification rate, and the reaction temperature under the high-temperature reaction condition is the decisive factor influencing the denitrification. The denitrification rate can reach more than 95 percent at the temperature of more than 340 ℃, and the higher denitrification rate can be reached by prolonging the reaction time under the low-temperature condition.

The coke oven gas containing 40-60% of hydrogen is difficult to separate hydrogen in the process after coking. Resulting in waste of hydrogen resources.

In a word, distilled raw gas is coked at a carbonization chamber, an ascending pipe and a bridge pipe, raw gas resources are wasted, great hidden dangers are brought to safe production, the labor intensity and difficulty of equipment maintenance and repair in the production process are increased, and the coke oven productivity is reduced because macromolecule raw gas is cracked, meanwhile, hydrogenation is needed in the lightening processing of coal tar, 40-60% of hydrogen resources in the coal gas cannot be applied, and a plurality of technical difficulties and pain points exist in the coke oven process:

1. the cracking reaction of macromolecular coal tar can cause a large amount of deposited carbon to be attached to the top of the carbonization chamber, the ascending pipe and the bridge pipe, thereby bringing great hidden danger to safe production and increasing the labor intensity and difficulty of equipment maintenance in the production process;

2. the coal tar contains sulfur and nitrogen which are difficult to remove, further utilization or combustion can generate sulfide and nitride environmental pollution, and the desulfurization and denitrification increase the process cost;

3. the graphite at the top of the carbonization chamber is burnt and decoked, which wastes energy and resources and reduces the productivity of the coke oven;

4. the yield of tar is reduced by cracking macromolecular coal tar, and the benefit is reduced;

5. the temperature of the raw coke gas low-temperature coke graphite is high, the energy consumption of the subsequent ammonia injection is wasted, and the waste heat is wasted.

SUMMERY OF THE UTILITY MODEL

The utility model aims to provide a membrane fixed bed catalyst riser for waste heat recovery and hydrogen utilization, which has the principle that after hydrogen-rich raw gas dried from a coking later-stage carbonization chamber of a coke oven is led into another carbonization chamber or riser pipe which is just added with coal according to the method of the patent application No. CN202010620326.X 'a coke oven hydrogen utilization method and a system thereof', macromolecule raw gas dried from coke coal which is newly added into the carbonization chamber is mixed with hydrogen-rich raw gas dried from another coking later-stage carbonization chamber, the mixed hydrogen-rich raw gas utilizes waste heat recovery to control the reaction temperature in the process of flowing out through a fixed bed catalyst riser pipe which utilizes a layer of membrane added with waste heat recovery and hydrogen, utilizes the riser pipe to contact the fixed bed catalyst on the surface of the raw gas for catalysis, and enables the hydrogen-rich raw gas to perform directional reaction under the proper temperature and the action of the catalyst, the technical bottleneck problem of the existing coke oven production process is eliminated. The reliability and the stability of the ascending pipe are improved, the long-term stable and safe operation of the system is facilitated, and particularly, the hot hydrogen resource of the system is comprehensively utilized.

The technical scheme of the utility model is as follows: a membrane type fixed bed catalyst crude gas waste heat recovery and hydrogen utilization ascending pipe comprises a shell of the ascending pipe and a bridge pipe tee joint (7), wherein hydrogen-rich crude gas is introduced into the ascending pipe, and the inner side of the shell of the ascending pipe comprises a cylinder wall heat-insulating layer (1), a temperature control and waste heat recovery device, an anti-corrosion ceramic layer (3) and a membrane type fixed bed catalyst layer (4); the inner layer of the pipe wall of the shell of the ascending pipe is a cylinder wall insulating layer (1), a temperature control and waste heat recovery device is arranged in the cylinder wall insulating layer (1), and a working medium for taking away waste heat of raw coke oven gas is introduced into the temperature control and waste heat recovery device; and the outer surface of the temperature control and waste heat recovery device is adhered with an anticorrosive ceramic layer (3), or is adhered with a mixed layer combining the anticorrosive ceramic layer (3) and a membrane type fixed bed catalyst layer (4), when the outer surface of the temperature control and waste heat recovery device is independently adhered with the anticorrosive ceramic layer (3), the outer surface of the temperature control and waste heat recovery device contacted with the hydrogen-rich raw gas is also adhered with the membrane type fixed bed catalyst layer (4).

As a preferred embodiment of the present invention, the temperature control and waste heat recovery device is a cylindrical wall temperature control and waste heat recovery device (2) and/or a central temperature control and waste heat recovery device (6); when the temperature control and waste heat recovery device is the cylinder wall temperature control and waste heat recovery device (2), the cylinder wall temperature control and waste heat recovery device (2) is arranged on the inner layer of the cylinder wall heat preservation layer (1), and when the temperature control and waste heat recovery device is the central temperature control and waste heat recovery device (6), the central temperature control and waste heat recovery device (6) is arranged in the radial outward arrangement direction of the center of the ascending pipe shell, and the position is ensured to be the position where the raw coal airflow field and the temperature field are uniform.

The utility model further comprises a stirring device (5) arranged in the center of the shell of the ascending pipe, wherein the stirring device (5) can realize the function of rotating or moving parts, and the turbulence degree of the raw gas is strengthened by stirring the raw gas through the rotation or movement of the parts.

In a preferred embodiment of the utility model, the stirring device (5) is arranged at the center of the riser, the stirring device (5) is provided with guide vanes, the surface of the stirring device (5) is adhered with an anticorrosive ceramic layer (3), the outer layer of the anticorrosive ceramic layer (3) is adhered with a membrane type fixed bed catalyst layer (4), or a mixed layer which is formed by combining the anticorrosive ceramic layer (3) and the membrane type fixed bed catalyst layer (4) into a whole is adhered.

As a preferred embodiment of the utility model, the inner surface of the bridge pipe tee joint (7) is attached with a membrane type fixed bed catalyst layer (4), or the local inner surface of the bridge pipe tee joint (7) is attached with the membrane type fixed bed catalyst layer (4).

As a preferred embodiment of the utility model, the method also comprises adding a mesh type fixed bed inside the ascending pipe or on the top of the carbonization chamber.

As a preferred embodiment of the utility model, the method also comprises the step of attaching a membrane type fixed bed catalyst layer (4) to the surface of the internal framework (8) of the riser.

The utility model has the technical effects that:

compared with the prior art, the membrane type fixed bed catalyst raw gas waste heat recovery and hydrogen utilization ascending tube has the following advantages:

1. the coke oven hydrogen utilizes the control, adjustment and induction of the cracking reaction of macromolecular coal tar, so that the adhesion of deposited carbon at the top of the carbonization chamber is eliminated;

2. the addition of the fixed bed catalyst layer can promote the hydrogenation target reaction, promote the lightening of macromolecules after cracking, increase the light yield and improve the added value of coal tar.

3. The utility model realizes proper hydrogenation reaction through hydrogen-rich cracking control, so that macromolecule coal tar is cracked and hydrogenated, the yield of the coal tar is improved, and the coking benefit is obviously improved.

4. The utility model can lead organic sulfur in the raw gas to form inorganic sulfur through hydrogenation reaction, is easy to adopt a chemical method for desulfurization and denitrification, reduces the environmental pollution and lowers the coke oven or tar deep processing treatment cost.

5. The hydrogen-rich pipe duct provided by the utility model is used for cooling waste heat recovery, and is energy-saving and emission-reducing.

6. The utility model reduces the temperature of the crude gas low-temperature coke graphite after lightening, can obviously reduce the injection amount of the subsequent ammonia, and improves the recovery amount of the waste heat.

7. According to the utility model, in the process of waste heat recovery and hydrogen gas utilization, the waste heat recovery is utilized to control the reaction temperature, and the riser is utilized to contact the membrane type fixed bed catalyst on the surface of the raw gas for catalysis, so that the hydrogen-rich raw gas can perform directional reaction at a proper temperature under the action of the catalyst, and the technical bottleneck problem of the existing coke oven production process is solved. The reliability and the stability of the ascending pipe are improved, and the long-term stable and safe operation of the system is facilitated.

8. The utility model can reduce the focus of the existing coke oven crude gas at 450 ℃, recover more waste heat of the crude gas, and reduce the mechanical energy consumption and the ammonia water consumption of the subsequent injection of high-pressure ammonia water; the membrane type fixed bed catalyst layer 4 is attached to the outer surface of the raw coke oven gas side anticorrosive ceramic layer 3 of the waste heat recovery temperature control device, when raw coke oven gas flows through the surface, hydrogen-rich raw coke oven gas can generate directional lightening reaction under the action of the membrane type fixed bed catalyst layer 4 on the surface, a target product is produced, the light yield of coal tar is improved, and the additional value of the coal tar is improved.

9. Under the catalytic action of an outer membrane type fixed bed catalyst layer 4 attached to a cylinder wall temperature control and waste heat recovery device 2, the directional reaction is carried out, the yield of tar light products is improved, the economic benefit is improved, the dew point temperature of raw coke gas is reduced, the waste heat capable of recovering the raw coke gas is reduced, the energy-saving benefit is improved, coking below a condensation temperature point is prevented, the waste heat above the condensation temperature point is saved by recycling, the spraying amount of cooling ammonia water is reduced, and the mechanical consumption of ammonia water circulation is saved.

Drawings

FIG. 1 is a schematic structural diagram of an embodiment of the present invention;

FIG. 2 is a schematic structural diagram of a second embodiment of the present invention;

FIG. 3 is a schematic diagram of a third embodiment of the present invention;

FIG. 4 is a diagram illustrating a fourth embodiment of the present invention;

FIG. 5 is a partial structural detail view of the present invention;

FIG. 6 is a schematic view of a framework of the present invention with a fixed bed catalyst layer attached to the surface thereof;

the device comprises a cylinder wall heat-insulating layer 1, a cylinder wall temperature control and waste heat recovery device 2, an anticorrosive ceramic layer 3, a fixed bed catalyst layer 4, a stirring device 5, a central temperature control and waste heat recovery device 6, a bridge pipe tee joint 7 and a framework 8.

Detailed Description

In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations. Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the utility model, as claimed, but is merely representative of selected embodiments of the utility model. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.

The utility model is further illustrated by the following specific examples in combination with the accompanying drawings.

As shown in the figures, a membrane type fixed bed catalyst crude gas waste heat recovery and hydrogen utilization riser comprises: the device comprises a cylinder wall heat-insulating layer 1, a temperature control and waste heat recovery device, an anticorrosive ceramic layer 3, a membrane type fixed bed catalyst layer 4, a stirring device 5 and a bridge pipe tee joint 7, wherein the anticorrosive ceramic layer 3 is attached to the outer surfaces of the temperature control and waste heat recovery device and the stirring device 5, or a mixed layer combining the anticorrosive ceramic layer 3 and the membrane type fixed bed catalyst layer 4 is attached to the outer surfaces of the temperature control and waste heat recovery device and the stirring device 5; the temperature control and waste heat recovery device is internally provided with a working medium which can take away waste heat, and the working medium is introduced with the working medium with proper temperature and pressure under the action of temperature control information to take out heat at the residual temperature above the reaction condition for waste heat recovery and utilization, so that the utility model can reduce the focus of the crude gas of the existing coke oven at 450 ℃, recover more waste heat of the crude gas and reduce the mechanical energy consumption and the ammonia water consumption of the subsequent injection of high-pressure ammonia water; the membrane type fixed bed catalyst layer 4 is attached to the outer surface of the raw coke oven gas side anticorrosive ceramic layer 3 of the waste heat recovery temperature control device, when raw coke oven gas flows through the surface, hydrogen-rich raw coke oven gas can generate directional lightening reaction under the action of the membrane type fixed bed catalyst layer 4 on the surface, a target product is produced, the light yield of coal tar is improved, and the additional value of the coal tar is improved. Different technical solutions can be formed by different combinations of the parts, and four embodiments are given below and are formed by different combinations of the various devices.

As shown in fig. 1 or 5, in a preferred embodiment, a first technical solution is that the temperature control and waste heat recovery device includes only a cylindrical wall including a cylindrical wall temperature control and waste heat recovery device 2: the cylinder wall temperature control and waste heat recovery device 2 is positioned in a cylinder body on the inner side of the ascending pipe shell and the heat insulation layer 1, an anticorrosive ceramic layer 3 is attached to the outer layer of the cylinder wall temperature control and waste heat recovery device 2, a fixed bed catalyst layer film 4 is attached to the outer surface of the anticorrosive ceramic layer 3, or a mixed layer formed by combining the anticorrosive ceramic layer 3 and the film type fixed bed catalyst layer 4 is attached to the outer layer, when crude gas flows through the inner side of the ascending pipe, a working medium for taking away waste heat of the crude gas flows through the cylinder wall temperature control and waste heat recovery device 2, the temperature is controlled through the inner cylinder wall temperature control and waste heat recovery device 2 on the pipe wall of the ascending pipe, and when the anticorrosive ceramic layer 3 is attached to the outer layer surface of the cylinder wall temperature control and waste heat recovery device 2, the film type fixed bed catalyst layer 4 is attached to one side in contact with the hydrogen-rich crude gas; when the hydrogen-rich raw gas flows through the cylinder wall, the raw gas is subjected to directional reaction under the catalytic action of an outer membrane type fixed bed catalyst layer 4 attached to the cylinder wall temperature control and waste heat recovery device 2, so that the yield of tar light products is improved, the economic benefit is improved, the dew point temperature of the raw gas is reduced, the waste heat capable of recovering the raw gas is reduced, the energy-saving benefit is improved, coking below a condensation temperature point is prevented, the waste heat below the condensation temperature point is saved by recycling, the spraying amount of cooling ammonia water is reduced, and the mechanical consumption of ammonia water circulation is saved.

As shown in fig. 2, in the second preferred embodiment, in order to include the temperature control and waste heat recovery device 2 and the stirring device 5, the stirring device 5 can implement a technical solution of rotating or moving components, the cylinder wall temperature control and waste heat recovery device 2 is positioned on the ascending pipe shell and the cylinder body at the inner side of the heat insulation layer 1, an anticorrosive ceramic layer 3 is attached to the outer layer of the temperature control and waste heat recovery device 2 on the cylinder wall, a fixed bed catalyst layer membrane 4 is attached to the anticorrosive ceramic layer 3, or a mixed layer which combines an anticorrosive ceramic layer 3 and a membrane type fixed bed catalyst layer 4 is attached to the outer layer of the cylinder wall temperature control and waste heat recovery device 2, when the outer surface of the cylinder wall temperature control and waste heat recovery device 2 is attached with an anticorrosive ceramic layer 3, one side close to the hydrogen-rich raw gas channel is attached with a membrane type fixed bed catalyst layer 4, when the raw gas flows through the inner surface of the ascending pipe, the raw gas is subjected to hydrocracking reaction under the action of the membrane type fixed bed catalyst layer 4, so that the raw gas is subjected to light-weight reaction. Meanwhile, a stirring device 5 is also arranged, as a specific embodiment of the utility model, a stirring rod or a guide vane can be arranged on the stirring device, or the stirring device is arranged in other rotating and vertical moving disturbance modes, so that the raw coke oven gas in the riser generates radial turbulence in the flowing process, the contact between the raw coke oven gas and the catalyst is increased, and the reaction is promoted to be carried out.

As a preferred embodiment of the utility model, the stirring device 5 can realize rotating or moving parts, the rotating or moving parts are driven by a motor positioned at the top of the ascending pipe, the stirring device 5 rotates or moves through the rotation of the central shaft to form the stirring of the raw coke oven gas, the purposes of strengthening the turbulence degree of the raw coke oven gas and increasing the reaction speed and the reaction depth are realized, the stirring device 5 can also play the role of online maintenance of the ascending pipe, and the central shaft can realize the rotating or moving.

In a preferred embodiment of the present invention, the stirring device 5 is provided with a rotating guide vane, the surface of the stirring device 5 is attached with the anticorrosive ceramic layer 3, the outer layer of the anticorrosive ceramic layer 3 is attached with the membrane type fixed bed catalyst layer 4, or the outer layer of the anticorrosive ceramic layer 3 is attached with the membrane type fixed bed catalyst layer 4.

As shown in fig. 3, a third preferred embodiment is a technical solution that includes a riser tube wall insulating layer 1, a temperature control and waste heat recovery device, an anticorrosive ceramic layer 3, a membrane-type fixed-bed catalyst layer 4, and a bridge pipe tee 7, where the temperature control and waste heat recovery device is located on the riser tube wall (see the tube wall temperature control and waste heat recovery device 2) + at a suitable position where the center of the riser tube is radially and outwardly disposed (see the central temperature control and waste heat recovery device 6); the suitable position of the radially outward arrangement of the center of the ascending pipe is the position of the radially outward raw coal airflow field and the uniform temperature field of the center of the ascending pipe.

As shown in fig. 4, a fourth preferred embodiment is a technical solution including a cylindrical wall insulating layer 1, a cylindrical wall temperature control and waste heat recovery device 2, an anticorrosive ceramic layer 3, a membrane type fixed bed catalyst layer 4, a stirring device 5, a central temperature control and waste heat recovery device 6, and a three-way bridge pipe 7, where the temperature control and waste heat recovery device is located on a pipe wall of an ascending pipe (see the cylindrical wall temperature control and waste heat recovery device 2) + at a suitable position where the center of the ascending pipe is radially and outwardly disposed (see the central temperature control and waste heat recovery device 6) + rotationally and movably perturbs the membrane type fixed bed catalyst layer 4, or a combination of any two of them; the stirring device 5 is arranged in the ascending tube inner barrel of the rotating and moving disturbance membrane type fixed bed catalyst layer 4, can rotate or move, and forms stirring of raw coke oven gas through rotation or movement, so that the turbulence intensity of the raw coke oven gas is strengthened. As a preferred embodiment of the utility model, the apparatus further comprises the addition of a mesh-type fixed bed inside the riser or at the top of the carbonization chamber.

FIG. 6 shows a schematic view of a fixed bed catalyst layer 4 of a membrane type attached to the surface of a framework 8. The framework 8 can be a net structure, a tray type or a packing type and is arranged in an ascending pipe which does not occupy a large flow area, so that the contact area of the raw coke oven gas and the catalyst is increased, and the hydrogenation reaction is promoted.

The cylinder wall heat-insulating layer 1, the temperature control and waste heat recovery device, the anticorrosive ceramic layer 3, the membrane type fixed bed catalyst layer 4, the stirring device 5 and the three-way bridge pipe 7 are all existing components, as a specific embodiment of the utility model, the cylinder wall heat-insulating layer 1 is realized by adopting high-temperature-resistant heat-insulating cotton, and the temperature control and waste heat recovery device is realized by adopting a coil pipe with a temperature adjusting system, or a jacket, or the jacket and the coil pipe (see the utility model patent: a high-efficiency waste heat recovery device for a coke oven ascending pipe and an anti-coking method thereof, patent application No. CN201611134129.7, or utility model patent: a heat storage type waste heat recovery device based on automatic control and a recovery method thereof, patent application No. CN 201410461904.4).

In the description herein, references to the description of the term "one embodiment," "some embodiments," "an illustrative embodiment," "an example," "a specific example," or "some examples" or the like mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the utility model. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.

While embodiments of the utility model have been shown and described, it will be understood by those of ordinary skill in the art that: various changes, modifications, substitutions and alterations can be made to the embodiments without departing from the principles and spirit of the utility model, the scope of which is defined by the claims and their equivalents.

Claims

1. A membrane type fixed bed catalyst crude gas waste heat recovery and hydrogen utilization ascending pipe comprises a shell of the ascending pipe and a bridge pipe tee joint (7), wherein hydrogen-rich crude gas is introduced into the ascending pipe, and the membrane type fixed bed catalyst layer is characterized in that the inner side of the shell of the ascending pipe comprises a cylinder wall heat-insulating layer (1), a temperature control and waste heat recovery device, an anti-corrosion ceramic layer (3) and a membrane type fixed bed catalyst layer (4); the inner layer of the pipe wall of the shell of the ascending pipe is a cylinder wall insulating layer (1), a temperature control and waste heat recovery device is arranged in the cylinder wall insulating layer (1), and a working medium for taking away waste heat of raw coke oven gas is introduced into the temperature control and waste heat recovery device; and an anticorrosive ceramic layer (3) is attached to the outer surface of the temperature control and waste heat recovery device, and when the anticorrosive ceramic layer (3) is attached to the outer surface of the temperature control and waste heat recovery device alone, a membrane type fixed bed catalyst layer (4) is attached to the outer surface of the temperature control and waste heat recovery device contacting with the hydrogen-rich raw gas.

2. The membrane type fixed bed catalyst raw gas waste heat recovery and hydrogen utilization riser according to claim 1, characterized in that: the temperature control and waste heat recovery device is a cylinder wall temperature control and waste heat recovery device (2) and/or a central temperature control and waste heat recovery device (6); when the temperature control and waste heat recovery device is the cylinder wall temperature control and waste heat recovery device (2), the cylinder wall temperature control and waste heat recovery device (2) is arranged at a position close to the inner layer of the cylinder wall heat preservation layer (1), when the temperature control and waste heat recovery device is the central temperature control and waste heat recovery device (6), the central temperature control and waste heat recovery device (6) is arranged in the radial outward arrangement direction of the center of the ascending pipe shell, and the position is ensured to be the position where the ascending pipe center radially outward raw coal airflow field and the temperature field are uniform.

3. The membrane type fixed bed catalyst raw gas waste heat recovery and hydrogen utilization riser according to claim 1 or 2, characterized in that: the gas-liquid separator further comprises a stirring device (5) arranged in the center of the shell of the ascending pipe, the stirring device (5) can realize the function of rotating or moving parts, and the raw coke oven gas is stirred through the rotation or movement of the parts, so that the turbulence intensity of the raw coke oven gas is strengthened.

4. The membrane type fixed bed catalyst raw gas waste heat recovery and hydrogen utilization riser according to claim 3, characterized in that: agitating unit (5) set up at tedge center, are equipped with guide vane on agitating unit (5), and agitating unit (5) surface adheres to anticorrosive ceramic layer (3), and anticorrosive ceramic layer (3) skin reattachment diaphragm type fixed bed catalyst layer (4).

5. The membrane type fixed bed catalyst raw gas waste heat recovery and hydrogen utilization riser according to claim 1, characterized in that: the inner surface of the bridge pipe tee joint (7) is attached with a membrane type fixed bed catalyst layer (4), or the local inner surface of the bridge pipe tee joint (7) is attached with the membrane type fixed bed catalyst layer (4).

6. The membrane type fixed bed catalyst raw gas waste heat recovery and hydrogen utilization riser according to claim 1, characterized in that: and a screen type fixed bed is added in the ascending pipe or on the top of the carbonization chamber.

7. The membrane type fixed bed catalyst raw gas waste heat recovery and hydrogen utilization riser according to claim 1, characterized in that: also comprises a membrane type fixed bed catalyst layer (4) attached to the surface of an internal framework (8) of the ascending pipe.