CN214496142U - Separation device for synthesizing aromatic hydrocarbon product from methylbenzene and methanol - Google Patents
Separation device for synthesizing aromatic hydrocarbon product from methylbenzene and methanol Download PDFInfo
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- CN214496142U CN214496142U CN202120373651.0U CN202120373651U CN214496142U CN 214496142 U CN214496142 U CN 214496142U CN 202120373651 U CN202120373651 U CN 202120373651U CN 214496142 U CN214496142 U CN 214496142U
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Abstract
The utility model relates to a separator of toluene and methyl alcohol synthetic aromatic hydrocarbon product, include: the device comprises an isolation tower, a separation tower, a gas-liquid separation device, a supercharging device and a pressure swing adsorption device; the tower top material outlet of the isolation tower is connected with the tower middle material inlet of the separation tower; a discharge port at the top of the separation tower is connected with a feed inlet of the supercharging device; a discharge port at the top of the separation tower is connected with a feed inlet of the gas-liquid separation device; the discharge hole of the supercharging device is respectively connected with the feed inlet in the separation tower, the feed inlet of the gas-liquid separation device and the feed inlet of the pressure swing adsorption device; the discharge port of the gas-liquid separation device is respectively connected with the feed port of the pressure boosting device and the feed port of the pressure swing adsorption device. The existing separation system for synthesizing aromatic hydrocarbon products by toluene and methanol is redesigned, so that the number of equipment is reduced, the energy is saved by over 55 percent under the condition of realizing the same separation index with the prior art, and the investment can be reduced to 75 percent of the investment in the prior art.
Description
Technical Field
The utility model relates to a chemical product apparatus for producing technical field, concretely relates to separator of toluene and methyl alcohol synthetic aromatic hydrocarbon result.
Background
The alkylation of toluene and methanol is used as a new technology for producing xylene, and has the main advantages that the toluene raw material can be converted into a xylene product to the maximum extent, compared with the traditional toluene disproportionation technology for increasing the yield of xylene by using toluene, the toluene disproportionation technology has the characteristic of high utilization rate of benzene rings, and is also a technology for high-value utilization of methanol.
In order to maximize the economic benefit of the production route, the toluene methanol fixed bed catalyst mainly acts on a shape selective methylation technology, the selectivity of paraxylene in mixed xylene is greatly improved through the process technology, the mass fraction of paraxylene in the produced xylene is up to more than 90%, and the subsequent paraxylene separation cost is greatly reduced. Therefore, the technology for preparing aromatic hydrocarbon by toluene methanol alkylation reaction can possibly upgrade or replace the existing integrated device which takes disproportionation reaction and adsorption separation as core aromatic hydrocarbon. For example, CN111072445A discloses a process for synthesizing xylene from toluene and methanol, which comprises the following reaction steps: conveying toluene and methanol into a toluene and methanol mixing tank for mixing, heating and gasifying the toluene and methanol mixture through a heater, mixing the mixture with hydrogen from a hydrogen supply system, feeding the mixture into a fixed bed reactor, and reacting the toluene and methanol under the action of a solid acid catalyst to obtain a reaction material flow, wherein the reaction material flow contains xylene, unreacted toluene, a byproduct heavy aromatic hydrocarbon and a byproduct benzene; the separation area comprises the following process steps: the method comprises the following steps of enabling a reactant to pass through a gas-liquid separation tank to carry out gas-liquid separation to obtain a liquid phase material flow, enabling the liquid phase material flow to pass through a liquid-liquid separation tank to carry out liquid-liquid separation to obtain an oil phase material flow, enabling the oil phase material flow to enter a rectification module, separating the oil phase material flow through the rectification module to obtain dimethylbenzene, byproduct heavy aromatic hydrocarbon, byproduct benzene and unreacted methylbenzene, and enabling the dimethylbenzene to enter a product storage tank.
CN107602321A discloses a fluidized bed process method for producing p-xylene from benzene and methanol, which comprises the following steps: (1) the mixed raw material of benzene and methanol enters a reactor of the 1 st section after being preheated to contact with a catalyst, and gas phase mixture flows containing toluene, xylene, C1-C5, aromatic hydrocarbons with the carbon number not less than C9 and the like are generated. (2) The mixture flow and fresh methanol are mixed and enter a 2 nd stage reactor to contact with a catalyst to produce the paraxylene. (3) The toluene and unreacted benzene in the product are returned to the reactor of the 1 st section, alkylation reaction is continued, finally, the equilibrium composition of xylene, C1-C5, aromatic hydrocarbons which are not less than C9 and the like is formed, and the mixture flows out of the reaction system. The catalyst used in the steps is the same catalyst, the catalyst regeneration can be realized in the same regenerator, and the process is simple. The method well solves the contradiction between the benzene conversion rate and the lever balance of the p-xylene selectivity, so that the conversion rate per pass of benzene reaches more than 77 percent, and the selectivity of the p-xylene in isomers of the benzene reaches more than 84 percent.
The advantage of toluene and methanol to para-xylene is that the product has high para-xylene selectivity and a targeted separation process is required. The specificity of the product is as follows:
(1) the toluene content is relatively high, because the toluene conversion rate of the toluene methanol fixed bed reaction is relatively low and is in the range of 5-30%, the toluene content in the product is relatively high, and the purity of toluene in the circulating reaction is higher than that of the disproportionation reaction;
(2) the content of p-xylene in C8 aromatic hydrocarbon and C9 aromatic hydrocarbon is more than 93 percent, so that the separation ensures the complete removal of toluene, and mixed C-octaaromatic hydrocarbon and a small amount of C-nonaaromatic hydrocarbon in the subsequent operation can directly enter a crystallization separation unit;
(3) the content of the noncondensable gas in the reaction varies depending on the reaction time, the catalyst performance, the three-phase separation conditions, and the like, and the content of the noncondensable gas in the purification portion varies, and therefore, it is necessary to adjust the separation step.
Although toluene and methanol can realize the high-efficiency output of xylene products, the prior xylene product separation process still has the problems of high energy consumption, high investment, more equipment quantity and the like.
SUMMERY OF THE UTILITY MODEL
In view of the problem that exists among the prior art, one of the purposes of the utility model is to provide a separator of toluene and methyl alcohol synthetic aromatic hydrocarbon product, realized the reduction of energy consumption among toluene and the methyl alcohol synthetic aromatic hydrocarbon product, energy-conservation can reach more than 55%, is showing the investment that reduces equipment simultaneously, realizes with prior art under the same separation index, can reduce prior art's investment at least to 75%.
To achieve the purpose, the utility model adopts the following technical proposal:
the utility model provides a separator of toluene and methyl alcohol synthetic aromatic hydrocarbon product, separator of toluene and methyl alcohol synthetic aromatic hydrocarbon product includes: the device comprises an isolation tower, a separation tower, a gas-liquid separation device, a supercharging device and a pressure swing adsorption device;
the tower top material outlet of the isolation tower is connected with the tower middle material inlet of the separation tower;
a discharge hole at the top of the separation tower is respectively connected with a feed inlet of the supercharging device and a feed inlet of the gas-liquid separation device;
the discharge hole of the supercharging device is respectively connected with the feed inlet in the separation tower, the feed inlet of the gas-liquid separation device and the feed inlet of the pressure swing adsorption device;
the discharge hole of the gas-liquid separation device is respectively connected with the feed inlet of the supercharging device and the feed inlet of the pressure swing adsorption device;
a first valve is arranged between a discharge hole at the top of the separation tower and a feed inlet of the supercharging device;
a second valve is arranged between the discharge hole at the top of the separation tower and the feed inlet of the gas-liquid separation device;
a third valve and a fourth valve are respectively arranged between the discharge hole of the supercharging device and the feed inlet of the gas-liquid separation device and the feed inlet of the pressure swing adsorption device;
a fifth valve and a sixth valve are arranged between the discharge hole of the gas-liquid separation device and the feed inlet of the pressure boosting device and the feed inlet of the pressure swing adsorption device;
a first material outlet arranged at the bottom of the separation tower is connected with a first heat exchanger;
the first outlet of the first heat exchanger is connected with the inlet of the bottom of the separation tower;
and a discharge hole of the gas-liquid separation device is respectively connected with the fifth valve and the sixth valve through a first heat exchanger.
The utility model provides a separation device, to toluene methanol alkylation fixed bed reactor product (containing a large amount of benzene in the traditional toluene disproportionation reaction product, heavy aromatics such as C9+, contain a large amount of low carbon olefin alkane in the moving bed reaction product) separation, wherein toluene content is at 60-80% in the product, rich p-xylene mixed aromatics is at 20-35%, benzene content is at 1-20%, the remaining light component is ethane, toluene of low carbon light alkanes such as propane and the arene product of the xylene of methyl alcohol, through redesign to the existing separation system of toluene and methyl alcohol synthetic arene product, utilize the isolation tower, the knockout tower, the reduction of rectifying column and accessory equipment quantity has been realized to the coupling relation between gas-liquid separation device and the supercharging device, thereby reduce project investment and energy consumption, energy conservation can reach more than 55%, simultaneously show the investment that reduces equipment, the investment can be reduced to 75 percent of the investment of the prior art under the condition of realizing the same separation index as the prior art.
The utility model discloses in, partition tower and benzene knockout tower can adopt plate tower or packed tower.
The utility model discloses in, the product of isolating tower gets into the composition according to benzene and noncondensable gas after the knockout tower, if exceed 15% can adopt the compressor pressure boost intensification to provide the heat for the tower cauldron, the compression ratio is at 6-10, after relief pressure valve, condenser, get into gas-liquid separation device, the arene of condensation flows back to the knockout tower top, the gaseous phase gets into PSA purification device as noncondensable gas (control second valve, fourth valve and fifth valve open, first valve, third valve and sixth valve close); if the composition of benzene and non-condensable gas is relatively low, the aromatic hydrocarbon can be fully refluxed by adopting condensation at the top of the tower, the non-condensable gas is discharged from the top of the tower, and then a high-purity benzene product is extracted from a side line. And the toluene extracted from the tower kettle of the benzene separation tower and the toluene extracted from the side line of the partition wall separation tower are circulated to the reaction inlet together, at the moment, the first valve, the third valve and the sixth valve are opened, and the second valve, the fourth valve and the fifth valve are closed.
As the preferable technical proposal of the utility model, a material inlet of aromatic hydrocarbon products is arranged in the tower of the isolation tower;
a toluene discharge hole is formed in the tower of the isolation tower;
and a paraxylene material outlet is formed at the bottom of the isolation tower.
As the preferable technical proposal of the utility model, the bottom of the separation tower is provided with a second material outlet;
and the second material outlet is a toluene discharge outlet.
As a preferred technical solution of the present invention, a seventh valve and a second heat exchanger are sequentially disposed between the first heat exchanger and the fifth valve and between the first heat exchanger and the sixth valve;
the seventh valve comprises a pressure reducing valve.
As the preferred technical scheme of the utility model, the first export of second heat exchanger with the fifth valve is connected.
As the preferred technical scheme of the utility model, the second export of second heat exchanger with the sixth valve is connected.
As a preferred technical solution of the present invention, the first valve includes a ball valve or an electrically controlled valve;
the second valve comprises a ball valve or an electrically controlled valve.
As a preferred technical solution of the present invention, the third valve includes a ball valve or an electrically controlled valve;
the fourth valve comprises a ball valve or an electrically controlled valve.
As a preferred technical solution of the present invention, the fifth valve includes a ball valve or an electrically controlled valve;
the sixth valve comprises a ball valve or an electrically controlled valve.
As a preferred technical solution of the present invention, the first valve, the second valve, the third valve, the fourth valve, the fifth valve and the sixth valve are all connected to the PLC controller by using an electrically controlled valve;
a C6 organic matter detection device is arranged between the tower top material outlet of the isolation tower and the tower middle material inlet of the separation tower;
and the organic matter detection device not larger than C6 is connected with the PLC.
The device provided by the utility model, the concentration of the toluene extracted from the isolation tower is required to be 98-99.99%.
In the utility model discloses in, the bulkhead tower sets up a vertical wall in the rectifying column, also can extend to the top of the tower or the tower cauldron with the vertical wall. The utility model discloses in, set up the baffle in the next door tower and divide into four rectification regions next door tower inside, baffle upper portion is public rectification section, and the baffle lower part is public stripping section, and the left and right sides of baffle is two parts respectively, and wherein one side is the feeding section, carries out preliminary separation to the feeding, and the opposite side is ejection of compact section, and high-purity toluene is extracted to main siding, and its concentration is 98-99.99%; the bottom of the tower is carbon octa-arene rich in paraxylene and a small amount of carbon nonaarene.
Compared with the prior art, the utility model discloses following beneficial effect has at least:
(1) according to the product composition under different reaction conditions, the mixed solution of benzene, toluene and high-concentration p-xylene mixed C8 can be obtained on the basis of not increasing equipment, meanwhile, the energy consumption and equipment investment are greatly reduced, the occupied area is small, the operating cost and the equipment investment are reduced, and the energy consumption is reduced by more than 55%.
(3) The utilization of the partition tower can ensure the purity of toluene and xylene at the same time, the toluene can be directly reacted for recycling, the xylene-rich mixed liquid can directly enter downstream crystallization separation equipment, the matching sequence of the regulation and control device is determined according to the content of benzene and light components in the separation tower, the energy-saving technology is optimized, and the energy consumption is reduced.
Drawings
FIG. 1 is a schematic diagram of a separation device for synthesizing aromatic hydrocarbon products from toluene and methanol according to an embodiment of the present invention.
In the figure: 1-an isolation tower, 2-a separation tower, 3-a gas-liquid separation device, 4-a first valve, 5-a fourth valve, 6-a third valve, 7-a fifth valve, 8-a second valve, 9-a pressure boosting device, 10-a first heat exchanger, 11-a sixth valve, 12-a pressure swing adsorption device, 13-a second heat exchanger, 14-a seventh valve;
i-xylene aromatic hydrocarbon products after the reaction of toluene and methanol, II-benzene, a mixture of toluene and light components, III-p-xylene mixed aromatic hydrocarbon, IV-toluene, a overtime obtained by a V-separation tower, VI-benzene, VII-a circulating liquid phase of the separation tower, VIII-a gas phase at the top of the separation tower after pressurization, and IX-noncondensable gas.
The present invention will be described in further detail below. However, the following examples are only simple examples of the present invention, and do not represent or limit the scope of the present invention, which is defined by the appended claims.
Detailed Description
To better illustrate the present invention, facilitating the understanding of the technical solutions of the present invention, typical but not limiting embodiments of the present invention are as follows:
examples
This example provides a separation apparatus for synthesizing aromatic hydrocarbon products from toluene and methanol, as shown in fig. 1, the separation apparatus for synthesizing aromatic hydrocarbon products from toluene and methanol includes: the system comprises an isolation tower 1, a separation tower 2, a gas-liquid separation device 3, a supercharging device 9 and a pressure swing adsorption device 12;
the tower top material outlet of the isolation tower 1 is connected with the tower middle material inlet of the separation tower 2;
a discharge hole at the top of the separation tower 2 is connected with a feed inlet of the gas-liquid separation device 3;
a discharge hole at the top of the separation tower 2 is connected with a feed inlet of the supercharging device 9;
the discharge hole of the gas-liquid separation device 3 is respectively connected with the feed hole in the separation tower 2, the feed hole of the pressure boosting device 9 and the feed hole of the pressure swing adsorption device 12;
the discharge hole of the supercharging device 9 is respectively connected with the feed hole of the gas-liquid separation device 3 and the feed hole of the pressure swing adsorption device 12;
a first valve 4 is arranged between the discharge hole at the top of the separation tower 2 and the feed inlet of the gas-liquid separation device 3;
a second valve 8 is arranged between the discharge hole at the top of the separation tower 2 and the feed inlet of the supercharging device 9;
a third valve 6 and a fourth valve 5 are respectively arranged between the discharge hole of the gas-liquid separation device 3 and the feed hole of the pressure boosting device 9 and the feed hole of the pressure swing adsorption device 12;
a fifth valve 7 and a sixth valve 11 are arranged between the discharge hole of the supercharging device 9 and the feed hole of the gas-liquid separation device 3 and the feed hole of the pressure swing adsorption device 12;
a first material outlet arranged at the bottom of the separation tower 2 is connected with a first heat exchanger 10;
a first outlet of the first heat exchanger 10 is connected with an inlet at the bottom of the separation tower 2;
and the discharge port of the gas-liquid separation device 3 is respectively connected with the fifth valve 7 and the sixth valve 11 through a first heat exchanger 10.
A material inlet of an aromatic hydrocarbon product is arranged in the tower of the isolation tower 1;
a toluene discharge hole is formed in the tower of the isolation tower 1;
and a paraxylene material outlet is arranged at the bottom of the isolation tower 1.
A second material outlet is formed at the bottom of the separation tower 2;
and the second material outlet is a toluene discharge outlet.
A seventh valve 14 and a second heat exchanger 13 are sequentially arranged between the first heat exchanger 10 and the fifth valve 7 and between the first heat exchanger 10 and the sixth valve 11, the seventh valve 14 is a pressure reducing valve, a first outlet of the second heat exchanger 13 is connected with the fifth valve 7, and a second outlet of the second heat exchanger 13 is connected with the sixth valve 11.
The first valve 4 comprises a ball valve or an electrically controlled valve, the second valve 8 comprises a ball valve or an electrically controlled valve, the third valve 6 comprises a ball valve or an electrically controlled valve, the fourth valve 5 comprises a ball valve or an electrically controlled valve, the fifth valve 7 comprises a ball valve or an electrically controlled valve, and the sixth valve 11 comprises a ball valve or an electrically controlled valve; when the first valve 4, the second valve 8, the third valve 6, the fourth valve 5, the fifth valve 7 and the sixth valve 11 are all electric control valves, the valves are all connected with a PLC (programmable logic controller), at the moment, a C6 organic matter detection device is arranged between the tower top material outlet of the isolation tower 1 and the tower middle material inlet of the separation tower 2, and the C6 organic matter detection device is connected with the PLC, so that the interlocking control of feeding of different components is realized.
Application example 1
The application example aims at 5 percent of benzene content, 10 percent of light components of non-condensable gas, 60 percent of toluene content and 25 percent of xylene content in a mixed aromatic hydrocarbon product, wherein the light components are light alkanes such as ethane, propane and the like; the content of p-xylene in C8 aromatic hydrocarbon is 95%.
The composition of benzene and non-condensable gas in the product of the obtained isolation tower accounts for 18% of the total material, at the moment, the second valve, the fourth valve and the fifth valve in the embodiment are opened, and the first valve, the third valve and the sixth valve are closed; controlling the compression ratio of the supercharging device to be 8; the material flow enters a gas-liquid separation device after passing through a pressure reducing valve and a condenser, condensed aromatic hydrocarbon flows back to the top of a separation tower, and a gas phase as non-condensable gas enters a pressure swing adsorption purification device
The purity of benzene extracted from the tower central line of the separation tower is 99%, the purity of toluene extracted from the tower central line of the partition wall tower is 98%, and the toluene content in the xylene mixture is lower than 1%, which both meet the downstream requirements on the purity of material flow. Compared with the separation process in the prior art, the energy is saved by 57 percent, and the equipment investment is reduced by 38 percent.
Application example 2
The application example aims at separating toluene and methanol alkylated mixed aromatic hydrocarbon products, the benzene content is 8%, the light component of non-condensable gas is 1%, the toluene content is 65%, and the xylene content is 25%, wherein the light component is light alkane such as ethane, propane and the like; the content of p-xylene in C8 aromatic hydrocarbon is 95%.
The composition of benzene and non-condensable gas in the product of the obtained isolation tower accounts for 8% of the total material, at the moment, the second valve, the fourth valve and the fifth valve in the embodiment are closed, and the first valve, the third valve and the sixth valve are opened;
the purity of benzene obtained by side line extraction of the separation tower is 99%, the purity of toluene extracted by side line extraction of the partition separation tower is 99%, and the toluene content in the xylene mixture is lower than 1%, which all meet the requirements of downstream on component purity. Compared with the separation process in the prior art, the energy is saved by 58 percent, and the equipment investment is reduced by 38 percent.
According to the above results, the utility model provides a separation device, to toluene content at 60-80%, rich p-xylene mixed aromatics is at 20-35%, benzene content is at 1-20%, the light component of surplus is ethane, the toluene of low carbon light alkane such as propane and the arene product of the compound xylene of methyl alcohol, through redesign to the existing separation system of toluene and the synthetic arene product of methyl alcohol, utilize the isolation tower, the knockout tower, the reduction of rectifying column and additional equipment quantity has been realized to the coupling relation between gas-liquid separation device and the supercharging device, thereby reduce project investment and energy consumption, it can reach more than 55% to save energy, show the investment that reduces equipment simultaneously, realize under the same separation index with prior art, can reduce to 75% of prior art's investment.
The applicant states that the present invention is described by the above embodiments, but the present invention is not limited to the above detailed structural features, i.e. the present invention can be implemented only by relying on the above detailed structural features. It should be clear to those skilled in the art that any modifications to the present invention, to the equivalent replacement of selected parts and the addition of auxiliary parts, the selection of specific modes, etc., all fall within the scope of protection and disclosure of the present invention.
The above detailed description describes the preferred embodiments of the present invention, but the present invention is not limited to the details of the above embodiments, and the technical idea of the present invention can be within the scope of the present invention, and can be right to the technical solution of the present invention, and these simple modifications all belong to the protection scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and in order to avoid unnecessary repetition, the present invention does not need to describe any combination of the features.
In addition, various embodiments of the present invention can be combined arbitrarily, and the disclosed content should be regarded as the present invention as long as it does not violate the idea of the present invention.
Claims (10)
1. A separation device for synthesizing aromatic hydrocarbon products from toluene and methanol is characterized by comprising the following components: the device comprises an isolation tower, a separation tower, a gas-liquid separation device, a supercharging device and a pressure swing adsorption device;
the tower top material outlet of the isolation tower is connected with the tower middle material inlet of the separation tower;
a discharge hole at the top of the separation tower is respectively connected with a feed inlet of the gas-liquid separation device and a feed inlet of the supercharging device;
the discharge hole of the gas-liquid separation device is respectively connected with the feed inlet in the separation tower, the feed inlet of the supercharging device and the feed inlet of the pressure swing adsorption device;
the discharge hole of the supercharging device is respectively connected with the feed inlet of the gas-liquid separation device and the feed inlet of the pressure swing adsorption device;
a first valve is arranged between a discharge hole at the top of the separation tower and a feed inlet of the gas-liquid separation device;
a second valve is arranged between the discharge hole at the top of the separation tower and the feed inlet of the supercharging device;
a third valve and a fourth valve are respectively arranged between the discharge hole of the gas-liquid separation device and the feed inlet of the supercharging device and the feed inlet of the pressure swing adsorption device;
a fifth valve and a sixth valve are arranged between the discharge hole of the supercharging device and the feed inlet of the gas-liquid separation device and the feed inlet of the pressure swing adsorption device;
a first material outlet arranged at the bottom of the separation tower is connected with a first heat exchanger;
the first outlet of the first heat exchanger is connected with the inlet of the bottom of the separation tower;
and a discharge hole of the gas-liquid separation device is respectively connected with the fifth valve and the sixth valve through a first heat exchanger.
2. The apparatus for separating an aromatic hydrocarbon product synthesized from toluene and methanol according to claim 1, wherein a material inlet for the aromatic hydrocarbon product is provided in the column of the separation column;
a toluene discharge hole is formed in the tower of the isolation tower;
and a paraxylene material outlet is formed at the bottom of the isolation tower.
3. The apparatus for separating an aromatic hydrocarbon product synthesized from toluene and methanol according to claim 1 or 2, wherein the bottom of the separation column is provided with a second material outlet;
and the second material outlet is a toluene discharge outlet.
4. The separation device for synthesizing aromatic hydrocarbon products from toluene and methanol according to claim 3, wherein a seventh valve and a second heat exchanger are arranged between the first heat exchanger and the fifth valve and between the first heat exchanger and the sixth valve in sequence;
the seventh valve comprises a pressure reducing valve.
5. The apparatus for separating toluene and methanol synthetic aromatic hydrocarbon product of claim 4 wherein the first outlet of the second heat exchanger is connected to the fifth valve.
6. The apparatus for separating toluene and methanol synthetic aromatic hydrocarbon product as claimed in claim 4, wherein the second outlet of said second heat exchanger is connected to said sixth valve.
7. The apparatus for separating a toluene and methanol synthetic aromatic hydrocarbon product as claimed in claim 1, wherein said first valve comprises a ball valve or an electrically controlled valve;
the second valve comprises a ball valve or an electrically controlled valve.
8. The apparatus for separating a toluene and methanol synthetic aromatic hydrocarbon product according to claim 1 or 7, wherein the third valve comprises a ball valve or an electrically controlled valve;
the fourth valve comprises a ball valve or an electrically controlled valve.
9. The apparatus for separating a toluene and methanol synthetic aromatic hydrocarbon product as claimed in claim 1, wherein said fifth valve comprises a ball valve or an electrically controlled valve;
the sixth valve comprises a ball valve or an electrically controlled valve.
10. The apparatus for separating an aromatic hydrocarbon product synthesized from toluene and methanol according to claim 1, wherein the first valve, the second valve, the third valve, the fourth valve, the fifth valve and the sixth valve are electrically controlled and connected to a PLC controller;
a C6 organic matter detection device is arranged between the tower top material outlet of the isolation tower and the tower middle material inlet of the separation tower;
and the organic matter detection device not larger than C6 is connected with the PLC.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112961022A (en) * | 2021-02-10 | 2021-06-15 | 中国海洋石油集团有限公司 | Separation device for synthesizing aromatic hydrocarbon product from methylbenzene and methanol |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112961022A (en) * | 2021-02-10 | 2021-06-15 | 中国海洋石油集团有限公司 | Separation device for synthesizing aromatic hydrocarbon product from methylbenzene and methanol |
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