CN206519140U - Shell and tube paste state bed reactor and reaction system - Google Patents
Shell and tube paste state bed reactor and reaction system Download PDFInfo
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- CN206519140U CN206519140U CN201720062656.5U CN201720062656U CN206519140U CN 206519140 U CN206519140 U CN 206519140U CN 201720062656 U CN201720062656 U CN 201720062656U CN 206519140 U CN206519140 U CN 206519140U
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Abstract
The utility model is related to a kind of shell and tube paste state bed reactor and reaction system.The shell and tube paste state bed reactor is used for the reactor that high concentration acetylene prepares ethene, including tactic air inlet section, tubulation distribution section and expanding reach, wherein, gas access is provided with the air inlet section, for reacting gas to be passed through into shell and tube paste state bed reactor；The tubulation distribution section is provided with multiple tubulations, is reacted for reacting gas in tubulation distribution section, prepares ethene, the multiple tubulation bottom is provided with gas distributor, stomata is distributed with thereon；Gas vent is provided with the top of the expanding reach.Each tubulation is a small slurry bed system in shell and tube paste state bed reactor described in the utility model, because the diameter of each tubulation is smaller, it is highly of a relatively high, it is more uniform that gas-liquid-solid three-phase can be mixed, add the residence time, gas-liquid flow field distribution is improved, enlarge-effect is reduced so that it is more abundant that reaction can be carried out.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry and specifically relates to utilize high concentration acetylene preparation ethylene field, concretely relates to shell and tube slurry bed reactor and application slurry bed reactor's reaction system.
Background
Ethylene is an important basic raw material in modern industry, is one of the chemicals with the largest world yield, is widely applied to the fields of national economy, people's life, national defense and the like, and is the parent of organic synthesis. In the face of shortage of petroleum resources and rising of international oil price, raw material sources become bottlenecks in development of ethylene industry, and are problems which people must solve before. Therefore, a new source and a new process technology for preparing ethylene by using a process method to replace petroleum as a raw material are researched and developed, and the dependence on petroleum can be relieved.
In the coal chemical industry, it has become a mature process to prepare acetylene from coal as a raw material by a calcium carbide process or from natural gas by a non-catalytic partial oxidation process. Acetylene is used as a raw material, and an ethylene product is obtained through a hydrogenation process under the action of a selective hydrogenation catalyst, so that the coal chemical industry route can be further expanded. Therefore, the development of a new process and a new technology for preparing ethylene by acetylene hydrogenation has wide application prospects.
The solid phase catalytic hydrogenation technology of low concentration acetylene gas is mature in the petroleum industry, is mainly used for removing acetylene impurities from ethylene, and uses a fixed bed reactor filled with a solid phase catalyst for gas-solid phase reaction. However, due to high acetylene activity and large heat release of hydrogenation reaction, even if a small amount of acetylene exists in the cracked gas, the traditional gas-solid fixed bed hydrogenation reactor still has the serious problems of large green oil generation amount, short catalyst cycle period, easy temperature runaway of the reactor and the like.
The conventional slurry bed reactor solves the problems to a certain extent, and has a simple structure, is easy to transfer heat, and produces ethylene products with wide application, so that the selective hydrogenation of high-concentration acetylene by using the slurry bed reactor becomes an important production line for preparing olefin. However, when acetylene is used for preparing ethylene in the traditional slurry bed reactor, gas, liquid and solid phases are not uniformly mixed, the contact time of reaction raw materials is short, the bed temperature in the reactor is uniform, and the temperature is not easy to control.
SUMMERY OF THE UTILITY MODEL
In order to overcome the problems, the utility model provides a shell and tube slurry bed reactor and reaction system for the inside temperature of reactor is even, increases reaction raw materials contact time, raises the efficiency.
The tube array type slurry bed reactor is used for preparing ethylene from high-concentration acetylene. The shell and tube slurry bed reactor comprises an air inlet section, a shell and tube distribution section and an expansion section which are arranged in sequence, wherein,
the gas inlet section is provided with a gas inlet for introducing reaction gas into the tubular slurry bed reactor;
the tube array distribution section is provided with a plurality of tube arrays for the reaction of the reaction gas in the tube array distribution section to prepare ethylene, and the bottoms of the plurality of tube arrays are provided with gas distributors on which gas holes are distributed;
and a gas outlet is formed in the top of the expansion section.
Furthermore, the shell pass is formed by a plurality of tubes in the tube array type slurry bed reactor and the area between the tubes, and a heat exchange medium is arranged in the shell pass.
Furthermore, the side surface of the lower part of the tube array distribution section is provided with a heat exchange medium inlet, and the side surface of the upper part of the tube array distribution section is provided with a heat exchange medium outlet, so that a heat exchange medium enters the shell pass from the heat exchange medium inlet and is discharged from the heat exchange medium outlet.
Specifically, a tube array communicating area is arranged above the gas distributor.
More specifically, the lower side of the expansion section is provided with a solvent inlet, and the side of the tube array communication area is provided with a discharge opening, so that the solvent and the catalyst enter the plurality of tube arrays from the solvent inlet and are discharged from the discharge opening.
Preferably, the upper end of the expansion section is provided with a metal demister.
Reaction system for utilize high concentration acetylene preparation ethylene. The reaction system comprises the tube array type slurry bed reactor, a condenser, a gas-liquid separator and a catalyst preparation tank, wherein,
the shell and tube slurry bed reactor is provided with a gas inlet, a gas outlet, a discharge port, a solvent inlet, a heat exchange medium inlet and a heat exchange medium outlet;
the condenser is provided with a high-temperature product gas inlet and a mixed gas outlet, and the high-temperature product gas inlet is connected with the gas outlet of the tubular slurry bed reactor;
the gas-liquid separator is provided with a mixed gas inlet, an ethylene outlet and a solvent outlet, and the mixed gas inlet is connected with the mixed gas outlet of the condenser;
the catalyst preparation tank is connected with a solvent inlet of the tubular slurry bed reactor.
Still further, the system further comprises a thermal medium reservoir and a pump; wherein,
one end of the heat medium storage tank is communicated with a heat exchange medium outlet of the tube type slurry bed reactor;
one end of the pump is connected with the other end of the heat medium storage tank, and the other end of the pump is communicated with a heat exchange medium inlet of the tube array type slurry bed reactor.
Preferably, the system further comprises a temperature control unit, which is arranged between the shell and tube slurry bed reactor and the pump and is used for controlling the temperature of the heat exchange medium entering the shell and tube slurry bed reactor.
Specifically, the temperature control unit comprises a heater, a cooler and a heat exchange medium bypass which are arranged in parallel.
The utility model has the advantages that:
each tube in the tube array type slurry bed reactor of the utility model is a small slurry bed, because the diameter of each tube is small, the height is relatively high, the gas, liquid and solid phases can be mixed more uniformly, the retention time is increased, the distribution of the gas, liquid and flow fields is improved, the amplification effect is reduced, and the reaction can be carried out more fully; in addition, the design of the tube array communicating area in the tube array slurry bed reactor can ensure the uniformity of the liquid level in each tube array and avoid gas short circuit.
In addition, the system of the utility model can realize the accurate control of the temperature of the solvent of the system and keep the temperature of the solvent relatively stable, thereby ensuring the stable operation of the whole system; moreover, the sensible heat of the liquid-phase solvent is utilized, the heat dissipation capacity is obviously improved, the heat generated by the selective hydrogenation of acetylene to ethylene can be quickly removed, the temperature of a reaction bed layer is reduced, and the conversion rate of acetylene and the selectivity of ethylene are improved. The system well solved in acetylene selectivity hydrogenation system ethylene reaction in the green oil yield of fixed bed reactor big, catalyst cycle is short, the reactor easily "temperature runaway" the problem, because the violent collision each other between the catalyst granule in the fluidized bed, cause the loss of catalyst, the difficulty of dust removal and because the abrasive action of solid particle, the serious problem of wearing and tearing of heat transfer component and reactor.
Drawings
Fig. 1 is a schematic structural diagram of a tube type slurry bed reactor according to the present invention.
Fig. 2 is a schematic structural diagram of the reaction system of the present invention.
Detailed Description
The invention will be described in more detail with reference to the following figures and examples, so that the aspects and advantages of the invention can be better understood. However, the specific embodiments and examples described below are for illustrative purposes only and are not intended to limit the present invention.
As shown in figure 1, the shell and tube slurry bed reactor 1 of the present invention is used as a reactor for preparing ethylene by selective hydrogenation of acetylene, and the slurry bed reactor 1 comprises a gas inlet section, a shell and tube distribution section and an expansion section.
As shown in FIG. 1, at the bottom of the reactor 1 is a gas inlet section, at the bottom of which there is a gas inlet 101 for the reaction gas into the reactor 1.
As shown in fig. 1, a tube array distribution section is arranged above the gas inlet section, a plurality of tubes 106 are arranged in the tube array distribution section, the inside of each tube array is a tube pass, the tube pass is a main reaction site for preparing ethylene from acetylene, a shell pass is formed by a plurality of tube arrays and the tube arrays in the tube array slurry bed reactor, and a heat exchange medium is arranged in the shell pass to provide heat for the tube arrays 106. At the bottom of each tube row 106 there is a gas distributor 107, which gas distributor 107 may be hemispherical; the air holes are uniformly distributed on the air distributor 107 and are vertical to the spherical surface; such a design ensures that the reactant gas can enter the tubes 106 from all directions, so that the gas is uniformly distributed. Wherein, optionally, the diameter of the tube array 106 is 30-100 mm, the center distance is 1-5 times of the tube diameter, and preferably, the center distance between the holes is 1.5 times. Optionally, the diameter of the air holes is 3-8 mm, the center distance is 1-5 times of the pipe diameter, and preferably, the center distance between the holes is 1.5-3 times.
As shown in fig. 1, a tube array communicating area 108 is provided at the upper end of the gas distributor 107, the cross section of the tube array communicating area 108 presents a shape like a Chinese character 'wang', and the heat exchange area of the shell side is also ensured while the communication of all the tube arrays 106 is ensured.
As shown in FIG. 1, a discharge opening 109 is provided at the side of the tubular communication section 108, and when the reactor 1 is stopped for discharge, the solvent is discharged from the discharge opening 109.
As shown in FIG. 1, in the upper part of the tube slurry bed reactor 1 is an expanded section, and a gas outlet 105 is provided at the top thereof. Below the expanded section there is a solvent inlet 104 for the passage of the solvent and catalyst required for the reaction into a plurality of tubes in the tube distribution section. A metal demister 110 is provided at an upper portion of the expansion section for filtering the solvent and the catalyst of the reaction. The main function of the expanded section is to reduce the gas velocity of the product gas, to allow solvents and the like entrained in the gas to be separated out and returned to the reactor 1, and then the product gas is led out from the gas outlet 105.
As shown in fig. 2, the reaction system of the present invention is used for preparing ethylene by using high concentration acetylene. The reaction system comprises the tube type slurry bed reactor 1, the gas-liquid separator 3 and the catalyst preparation tank 8.
As shown in fig. 2, the shell and tube slurry bed reactor 1 has a gas inlet 101, a gas outlet 105, a solvent inlet 104, a discharge port 109, a heat exchange medium inlet 102, and a heat exchange medium outlet 103.
As shown in fig. 2, the condenser has a high-temperature product gas inlet and a mixed gas outlet, and the high-temperature product gas inlet is connected with the gas outlet of the tubular slurry bed reactor.
As shown in fig. 2, the gas-liquid separator has a mixed gas inlet, an ethylene outlet and a solvent outlet, and the mixed gas inlet is connected to the mixed gas outlet of the condenser.
As shown in fig. 2, the catalyst preparation tank 8 is connected to the solvent inlet 104 of the shell and tube slurry bed reactor 1.
As shown in fig. 2, the system further comprises a thermal medium reservoir 4 and a pump 5. One end of the heat medium storage tank 4 is communicated with a heat exchange medium outlet 103 of the tubular slurry bed reactor 1; one end of the pump 5 is connected with the other end of the heat medium storage tank 4, and the other end of the pump 5 is connected with the heat exchange medium inlet 102 of the tubular slurry bed reactor 1.
As shown in fig. 2, the system further includes a temperature control unit, which is disposed between the tubular slurry bed reactor 1 and the pump 5, and is used for controlling the temperature of the heat exchange medium entering the tubular slurry bed reactor. The temperature control unit comprises a heater 6, a cooler 7 and a heat exchange medium bypass which are arranged in parallel.
The system is used for preparing ethylene from acetylene, and usually nitrogen is used as a gas source to replace the whole system; then, the catalyst and the solvent which are prepared in the catalyst preparation tank 8 are pumped into the tubular slurry bed reactor 1, and then the heater 6 of the temperature control unit is gradually started to gradually heat the heat transfer medium; when the temperature of the solvent in the reactor 1 reaches the target temperature and the system stably runs, the mixed gas of acetylene and hydrogen as the reaction gas enters the reactor 1 through a gas inlet 101 at the bottom of the tubular slurry bed reactor 1, the operating pressure of the reactor 1 is 0.15-0.45 MPa, and the temperature is 90-180 ℃. The reaction gas enters the gas inlet section and enters the tube array slurry bed reactor 1 through a gas distributor 107 at the bottom of each tube array 106. Since the holes of the gas distributor 107 are uniformly distributed, the reaction gas is uniformly dispersed into the solvent in the tubes 106. At the tube array distribution section, each tube array 106 is a small slurry bed reactor 1, and as the diameter of each tube array 106 is smaller and the height is relatively higher, gas, liquid and solid phases can be mixed more uniformly, so that the retention time is increased, the gas-liquid flow field distribution is improved, the amplification effect is reduced, and the reaction can be carried out more fully. After exiting the tube array 106, the product gas passes through the enlarged section of the reactor 1 and leaves the reactor 1 at the top gas outlet 105 of the reactor 1.
Cooling the product gas from the top of the reactor 1 by a condenser 2; then, the gas and the liquid such as the solvent are separated by the gas-liquid separator 3, the separated solvent and the catalyst are sent into the reactor 1 again through the solvent inlet 104 at the top of the reactor 1, and the separated gas is the product ethylene.
The shell and tube slurry bed reactor 1 utilizes a heat exchange medium to provide heat for reaction, namely indirect heat exchange, and a pump 5 is used for transferring the heat exchange medium from a heat medium storage tank 4 to a temperature control unit; the temperature control unit consists of three lines of a heater 6, a heat exchange medium bypass and a cooler 7 which are arranged in parallel, and can be regulated and controlled according to different working conditions required by the reactor 1; when the reaction system needs to be heated, the heater 6 and the heat exchange medium bypass are started, and the heating rate is controlled by adjusting the heat exchange power and the flow of the heat exchange medium in the heat exchange medium bypass; when the reactor 1 needs to transfer heat, the heating power, the flow of the heat exchange medium bypass and the cooling power can be simultaneously controlled to control the temperature of the heat medium to keep stable; when the reaction system needs to be cooled, the cooler 7 and the heat exchange medium bypass are started, and the cooling rate is controlled by adjusting the heat exchange power and the flow of the heat exchange medium in the heat exchange medium bypass; the temperature control unit can meet the requirements of various working conditions of the tubular slurry bed reactor 1 on the temperature of the reaction system.
It should be noted that the above-mentioned embodiments described with reference to the drawings are only intended to illustrate the present invention and not to limit the scope of the present invention, and those skilled in the art should understand that modifications or equivalent substitutions made on the present invention without departing from the spirit and scope of the present invention should be included in the scope of the present invention. Furthermore, unless the context indicates otherwise, words that appear in the singular include the plural and vice versa. Additionally, all or a portion of any embodiment may be utilized with all or a portion of any other embodiment, unless stated otherwise.
Claims (9)
1. A shell and tube slurry bed reactor used for preparing ethylene from high-concentration acetylene is characterized by comprising a gas inlet section, a shell and tube distribution section and an expansion section which are sequentially arranged, wherein,
the top of the expansion section is provided with a gas outlet;
the bottom of the gas inlet section is provided with a gas inlet for introducing reaction gas into the tubular slurry bed reactor;
the tubular column distribution section is provided with a plurality of tubular columns for the reaction of the reaction gas in the tubular column distribution section to prepare ethylene, the bottoms of the plurality of tubular columns are provided with gas distributors on which gas holes are distributed, the area between the plurality of tubular columns and the tubular columns in the tubular slurry bed reactor forms a shell side, and a heat exchange medium is arranged in the shell side.
2. The shell-and-tube slurry bed reactor according to claim 1, wherein the lower side of the shell-and-tube distribution section is provided with a heat exchange medium inlet, and the upper side is provided with a heat exchange medium outlet, and the shell-and-tube slurry bed reactor is used for introducing a heat exchange medium from the heat exchange medium inlet into the shell pass and discharging the heat exchange medium from the heat exchange medium outlet.
3. The shell and tube slurry bed reactor according to claim 1, wherein a shell and tube communicating zone is provided above the gas distributor.
4. The shell and tube slurry bed reactor of claim 3 wherein said expanded section is flanked on a lower portion by a solvent inlet and said shell and tube communication zone is flanked by a discharge opening for passing solvent and catalyst from said solvent inlet to said plurality of shell and tube for discharge from said discharge opening.
5. The shell and tube slurry bed reactor according to claim 1, wherein a metal demister is provided at an upper end of the expanded section.
6. A reaction system for producing ethylene using acetylene in high concentration, comprising a shell and tube slurry bed reactor according to any one of claims 1 to 5, a condenser, a gas-liquid separator and a catalyst preparation tank, wherein,
the shell and tube slurry bed reactor is provided with a gas inlet, a gas outlet, a solvent inlet, a discharge port, a heat exchange medium inlet and a heat exchange medium outlet;
the condenser is provided with a high-temperature product gas inlet and a mixed gas outlet, and the high-temperature product gas inlet is connected with the gas outlet of the tubular slurry bed reactor;
the gas-liquid separator is provided with a mixed gas inlet, an ethylene outlet and a solvent outlet, and the mixed gas inlet is connected with the mixed gas outlet of the condenser;
the catalyst preparation tank is connected with a solvent inlet of the tubular slurry bed reactor.
7. The reaction system of claim 6, wherein the system further comprises a thermal medium reservoir and a pump; wherein,
one end of the heat medium storage tank is communicated with a heat exchange medium outlet of the tube type slurry bed reactor;
one end of the pump is connected with the other end of the heat medium storage tank, and the other end of the pump is communicated with a heat exchange medium inlet of the tube array type slurry bed reactor.
8. The reaction system of claim 7, further comprising a temperature control unit disposed between the tubular slurry bed reactor and the pump for controlling the temperature of the heat exchange medium entering the tubular slurry bed reactor.
9. The reaction system of claim 8, wherein the temperature control unit comprises a heater, a cooler, and a heat exchange medium bypass arranged in parallel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720062656.5U CN206519140U (en) | 2017-01-19 | 2017-01-19 | Shell and tube paste state bed reactor and reaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720062656.5U CN206519140U (en) | 2017-01-19 | 2017-01-19 | Shell and tube paste state bed reactor and reaction system |
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| Publication Number | Publication Date |
|---|---|
| CN206519140U true CN206519140U (en) | 2017-09-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720062656.5U Expired - Fee Related CN206519140U (en) | 2017-01-19 | 2017-01-19 | Shell and tube paste state bed reactor and reaction system |
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| CN (1) | CN206519140U (en) |
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- 2017-01-19 CN CN201720062656.5U patent/CN206519140U/en not_active Expired - Fee Related
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| Date | Code | Title | Description |
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| GR01 | Patent grant | ||
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| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Multitubular slurry bed reactor and reaction system Effective date of registration: 20180322 Granted publication date: 20170926 Pledgee: The Bank of Beijing Limited by Share Ltd. Anwar Road Branch Pledgor: Shenwu Technology Group Co.,Ltd. Registration number: 2018990000210 |
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| PP01 | Preservation of patent right |
Effective date of registration: 20190121 Granted publication date: 20170926 |
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| PD01 | Discharge of preservation of patent |
Date of cancellation: 20220921 Granted publication date: 20170926 |
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| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170926 |