CN115353439A - Process and device for producing ethylbenzene by ethylene-containing dry gas-liquid phase method - Google Patents
Process and device for producing ethylbenzene by ethylene-containing dry gas-liquid phase method Download PDFInfo
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- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 title claims abstract description 194
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 164
- 239000005977 Ethylene Substances 0.000 title claims abstract description 164
- 238000000034 method Methods 0.000 title claims abstract description 128
- 239000007791 liquid phase Substances 0.000 title claims abstract description 78
- 239000007789 gas Substances 0.000 claims abstract description 171
- 238000010521 absorption reaction Methods 0.000 claims abstract description 145
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 105
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 101
- 239000002250 absorbent Substances 0.000 claims abstract description 96
- 230000002745 absorbent Effects 0.000 claims abstract description 95
- 238000005804 alkylation reaction Methods 0.000 claims abstract description 83
- 238000000926 separation method Methods 0.000 claims abstract description 44
- 239000002994 raw material Substances 0.000 claims abstract description 35
- 238000003795 desorption Methods 0.000 claims abstract description 31
- 239000012071 phase Substances 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000000463 material Substances 0.000 claims abstract description 24
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 173
- 239000000047 product Substances 0.000 claims description 61
- 230000029936 alkylation Effects 0.000 claims description 48
- 238000006243 chemical reaction Methods 0.000 claims description 27
- 239000007788 liquid Substances 0.000 claims description 22
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 18
- 239000007795 chemical reaction product Substances 0.000 claims description 18
- 238000011084 recovery Methods 0.000 claims description 13
- 238000005406 washing Methods 0.000 claims description 10
- 238000001035 drying Methods 0.000 claims description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 8
- ODLMAHJVESYWTB-UHFFFAOYSA-N propylbenzene Chemical compound CCCC1=CC=CC=C1 ODLMAHJVESYWTB-UHFFFAOYSA-N 0.000 claims description 8
- 239000001257 hydrogen Substances 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 5
- KVNYFPKFSJIPBJ-UHFFFAOYSA-N 1,2-diethylbenzene Chemical compound CCC1=CC=CC=C1CC KVNYFPKFSJIPBJ-UHFFFAOYSA-N 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 239000002737 fuel gas Substances 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 claims description 3
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 claims description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 description 23
- 230000003197 catalytic effect Effects 0.000 description 18
- 238000004519 manufacturing process Methods 0.000 description 14
- 238000005265 energy consumption Methods 0.000 description 7
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 230000005587 bubbling Effects 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 2
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000010555 transalkylation reaction Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 230000001934 delay Effects 0.000 description 1
- JMNDBSWHIXOJLR-UHFFFAOYSA-N ethylbenzene;styrene Chemical compound CCC1=CC=CC=C1.C=CC1=CC=CC=C1 JMNDBSWHIXOJLR-UHFFFAOYSA-N 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229920000515 polycarbonate Polymers 0.000 description 1
- 239000004417 polycarbonate Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a process and a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method in the technical field of petrochemical industry. According to the invention, the raw material ethylene-containing dry gas is washed by the water and then is pressurized, cooled and separated by the compressor, so that moisture in the gas can be separated from the gas phase, the gas phase after separation is absorbed by the propylene absorption tower, most of moisture in the gas phase is dissolved in the absorbent, the moisture in the absorbent is separated from the system in the absorbent buffer tank and the propylene desorption tower system, the moisture content in the tower top propylene-removing dry gas and the ethylene-rich gas at the top of the ethylene desorption tower is obviously reduced, and the two gases can be directly fed into the ethylene absorption tower without passing through a dryer to be absorbed and then are used as the feed materials for alkylation reaction.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a process and a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method.
Technical Field
Ethylbenzene is a feedstock for the production of styrene, primarily by dehydrogenation. The technological route for producing ethylbenzene mainly includes liquid phase method and gas phase method, the liquid phase method usually adopts pure ethylene route, and the gas phase method usually adopts dilute ethylene dry gas method route. The source of the ethylbenzene raw material is related to the economic benefit and development of enterprises, and the ethylbenzene is produced by fully utilizing the ethylene-containing dry gas of refineries, so that the method is beneficial to improving the economic benefit of the enterprises and promoting the rapid development of the ethylbenzene-styrene industry.
The refinery catalytic dry gas is used as tail gas of a catalytic device, and is generally directly used as fuel gas to be burnt, so that the utilization rate is low. The catalytic dry gas is rich in ethylene and can cause serious waste of ethylene resources when being used as fuel gas to be burnt, the utilization rate of the catalytic dry gas can be improved by utilizing the ethylene in the catalytic dry gas to prepare ethylbenzene, and the production cost of an ethylbenzene device can be effectively reduced. The gas phase process has high reaction temperature, more side reactions, more impurity components such as dimethylbenzene, propyl benzene and the like in the product, relatively poor quality of the ethylbenzene product and high energy consumption. The reaction conditions of the liquid phase method process are mild, and the quality of the ethylbenzene product is better and the energy consumption is lower than that of the ethylbenzene product produced by the gas phase method process. The catalytic dry gas contains a certain amount of ethylene components and also contains more components such as hydrogen, methane, ethane, nitrogen and the like, so that the alkylation reactor is difficult to operate under the liquid phase condition, and the liquid phase process catalyst is easy to coke and inactivate when a gas phase exists. At present, the industrialized device for preparing ethylbenzene by catalyzing dry gas in China mostly adopts a gas phase process route.
CN101665398A proposes a method for refining ethylene-containing raw gas for a process of preparing ethylbenzene from ethylene, which comprises three tower flows of an absorption tower, an ethylene desorption tower and a propylene desorption tower, wherein the absorption tower takes benzene as an absorbent, a saturated absorbent absorbing propylene in the raw gas sequentially enters the ethylene desorption tower and the propylene desorption tower, gas at the top of the ethylene desorption tower returns to an inlet of the absorption tower, and the absorbent desorbed in the propylene desorption tower returns to the absorption tower for recycling. The method can improve the propylene removal rate in the feed gas to more than 98% and the ethylene loss rate to less than 2% under the working condition that the volume content of the propylene in the feed gas is up to 3%. Solves the defects of discontinuous operation, high ethylene loss rate, low propylene removal rate and the like of the ethylene raw material gas pretreatment process in the prior art.
CN102746084A provides a raw material processing method for a process for preparing ethylbenzene from an ethylene-containing raw material, wherein the ethylene-containing raw material gas passes through an absorption-desorption device, the gas enters an ethylbenzene reaction part, the desorbed gas enters a liquid separation device after being cooled, part of condensate containing an absorbent and heavy hydrocarbon after liquid separation returns to the absorption-desorption device to be used as a circulating absorbent, and the other part of condensate is sent to a product separation part for processing.
CN106278797A provides a method for producing ethylbenzene by catalytic dry gas, which is a process for preparing ethylbenzene by a gas phase method, the catalytic dry gas containing ethylene enters catalyst bed layers of each section of an alkylation reactor in N strands after heat exchange, and the flow of each strand is the same; the raw material benzene is added into the alkylation reactor from the first section of the alkylation reactor or added into the alkylation reactor in N sections, and the flow rate of each section is the same. Ethylene and benzene react in each section of catalyst bed layer in a contact way, the inlet temperature of each section of catalyst bed layer is 300-400 ℃, and the temperature rise of the bed layer is 10-25 ℃. The method solves the problems of non-uniform temperature rise of a reactor bed layer, low ethylene recovery rate, low catalyst utilization rate and the like caused by large concentration change of ethylene contained in the catalytic dry gas in the prior art (such as CN200510105256.X, CN1557794A and the like) by controlling the inlet temperature of the catalytic dry gas. However, the process method has the problems of high benzene-olefin ratio, low ethylene conversion rate, high reaction temperature, a plurality of byproducts, high energy consumption, heating of a heating furnace at a benzene inlet and the like.
The catalytic dry gas-liquid phase method for preparing ethylbenzene mainly comprises two process flows. One is a bubbling bed process, in which the catalyst is completely immersed in benzene, and the catalytic dry gas is passed through the catalyst completely immersed in benzene in the form of bubbling, and reacted with benzene to produce ethylbenzene, then the ethylbenzene product is obtained by subsequent separation. The other method is to adopt a catalytic rectification process, wherein catalytic dry gas and fresh benzene respectively enter from the bottom and the top of the tower, the benzene absorbs the catalytic dry gas in the catalytic rectification tower and carries out alkylation reaction, the catalytic rectification tower usually adopts a plate tower or a packed tower, the catalyst is distributed in the tower, the tail gas (mainly comprising components such as hydrogen, methane, ethane, nitrogen and the like) after the reaction is discharged from the top of the tower, the mixture of ethylbenzene and benzene is obtained from the bottom of the tower, and then the mixture enters a subsequent device for separation to obtain an ethylbenzene product. The bubbling bed process completely submerges the catalyst, so that the catalyst can be protected to a certain extent, but the process has the defects of low conversion rate, poor selectivity, large catalyst consumption and the like due to low absorption efficiency of the bubbling bed. The catalytic rectification process has high absorption efficiency, high conversion rate, good selectivity and less catalyst consumption, but the process cannot ensure that the catalyst is not contacted with a gas phase completely, and the service life of the catalyst cannot be ensured.
CN102267859B provides a method for producing ethylbenzene from ethylene, which is a method for preparing ethylbenzene from liquid phase, wherein an alkylation reactor is provided with N absorption sections and N reaction sections, a mixture containing ethylene and inert components is divided into N parts which respectively enter the bottom of the N absorption section of the alkylation reactor, and the N parts are contacted with an absorbent from an absorbent inlet at the top of the alkylation reactor in the absorption sections and dissolved in the absorbent, and then flow downwards to enter the reaction sections to react to generate ethylbenzene and polyethylbenzene. The absorbent passes through each absorption section and each reaction section in turn in the alkylation reactor, the invention can obviously improve the conversion rate and the recovery rate of the ethylene, can effectively ensure that the reaction is carried out under the liquid phase condition, and avoids the direct contact of the gas-phase ethylene and the catalyst, but the absorbent has longer retention time in a catalyst bed layer, more side reactions and complicated reactor structure and is difficult to manufacture.
To sum up, the dry gas ethylbenzene production process applied in the current refinery industry is mainly a gas phase process, and the gas phase process has the problems of low ethylene recovery rate, a large amount of byproducts, high energy consumption and the like.
Disclosure of Invention
In order to solve the problems, the invention provides a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which aims to solve the technical problems of high energy consumption, low ethylene recovery rate, more byproducts, short catalyst operation period and the like in the conventional process for producing ethylbenzene by a dry gas method.
In order to achieve the purpose, the invention adopts the technical scheme that:
the process for producing ethylbenzene by the ethylene-containing dry gas-liquid phase method comprises the following steps:
1) Firstly, washing an ethylene-containing dry gas raw material from the upstream to remove carried trace impurities, then entering a dry gas compressor, boosting the pressure by the dry gas compressor, and then sending a gas phase to a propylene removal unit;
2) The ethylene-containing dry gas after being pressurized in the step 1) enters the middle part of a propylene absorption tower of a propylene removal unit and is in countercurrent contact with an absorbent entering from the top of the tower, the propylene-removal dry gas enters the ethylene absorption tower after coming out from the top of the propylene absorption tower, part of the absorbent is extracted from the middle section of the propylene absorption tower and exchanges heat with materials from the bottom of a propylene desorption tower, and the heat is recovered and then returned to the lower section of the propylene absorption tower; feeding the material at the bottom of the propylene absorption tower to a propylene desorption tower; returning the material at the bottom of the propylene desorption tower after the removal of the propylene as a circulating absorbent to the top of the propylene absorption tower, and sending the propylene-rich gas at the top of the propylene desorption tower out of the device;
3) Fresh benzene enters a mixer, is mixed with circulating benzene from a product separation unit, enters a benzene dryer, is subjected to micro water removal in the benzene dryer, and is sent to an alkylation reaction unit;
4) And 2) introducing the depropylene dry gas from the top of the propylene absorption tower in the step 2) into the lower part of an ethylene absorption tower of an alkylation reaction unit, and making the depropylene dry gas contact with lean cycle absorption liquid entering from the top of the ethylene absorption tower in a countercurrent manner, conveying absorption tail gas from the top of the ethylene absorption tower to a product separation unit, and introducing the rich cycle absorption liquid from the bottom of the ethylene absorption tower into an alkylation reactor after boosting and heat exchange by using a pump.
5) Exchanging heat between a reaction product from an alkylation reactor and a reactor feeding material, reducing pressure, entering a reaction product flash tank, allowing a gas phase from the top of the reaction product flash tank to pass through a flash gas heat exchanger, then entering an absorbent feeding tank for liquid separation, allowing an uncondensed gas phase to enter a deethanizer, allowing a part of a liquid phase material from the bottom of the flash tank to be used as lean cycle absorption liquid of an ethylene absorption tower and be sent to the absorbent feeding tank, allowing a dried mixed benzene from the benzene drying unit in the step 3) to also enter the absorbent feeding tank, and then increasing the pressure of the mixed benzene and the benzene by an absorbent booster pump and sending the mixed benzene to the ethylene absorption tower; the other part is sent to a subsequent product separation unit;
6) The ethane-rich gas obtained by the separation at the top of the deethanizer is sent out of the device, and the components at the bottom of the deethanizer are sent to a subsequent product separation unit.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: a drier is arranged before the propylene-removed dry gas enters the ethylene absorption tower in the step 2) to remove trace moisture existing in the propylene-removed dry gas in a phase equilibrium mode.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: the ethylene volume content of the ethylene-containing dry gas raw material in the step 1) is 5-95%, and the ethylene-containing dry gas raw material also contains trace MDEA impurities and H 2 、N 2 、O 2 、CO、CO 2 、CH 4 、C 2 H 4 、C 2 H 6 、C 3 H 6 、 C 3 H 8 One or more of C4+ and the like;
the invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: after the dry gas subjected to the propylene removal is dehydrated by a dryer, the water content in the dry gas subjected to the propylene removal after the drying is controlled to not more than 300ppm, and preferably the water content in the dry gas is controlled to not more than 100ppm.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: and 2) the absorbent is in countercurrent contact with the ethylene-containing dry gas in a propylene absorption tower to absorb propylene and heavy components in the ethylene-containing dry gas and also absorb a small amount of ethylene and other light components. The absorbent is one or more of benzene, ethylbenzene, methyl ethyl benzene and diethylbenzene. The propylene absorption tower has 10-50 theoretical plates, tower top pressure of 0.6-4.5 MPag, preferably 0.8-1.5 MPag, absorption temperature of 5-60 deg.c, preferably 15-20 deg.c, desorption temperature of 150-280 deg.c, preferably 160-240 deg.c.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: the de-propene dry gas at the top of the propene absorption tower also carries a small amount of absorbent, and the saturated absorbent absorbed at the bottom of the propene absorption tower mainly contains C 2 H 4 、C 2 H 6 And C 3 H 6 、C 3 H 8 C4+ and trace CH 4 、H 2 、N 2 、CO 2 And (4) and the like.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: the content of propylene in the dry gas from the top of the tower is controlled to not more than 300ppm by adjusting the absorption amount of the propylene absorption tower.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: the outlet pressure of the dry gas compressor in the step 1) is 1.2-3.0 MPag, preferably 1.5-2.5 MPag.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: and 4) the light component gas which is not absorbed at the top of the ethylene absorption tower enters a tail gas absorption tower of the product separation unit, after being absorbed by the heavy components such as ethylbenzene, polyethylbenzene or propylbenzene, methane hydrogen at the top of the tower is sent to a fuel gas pipe network or other devices for hydrogen recovery, and the liquid after absorption is sent to the product separation unit for benzene recovery. Or absorbing with polyethylbenzene, and directly feeding the absorbed liquid into a transalkylation reaction feed tank.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: step 4), pressurizing the liquid-phase material from the bottom of the ethylene absorption tower by a reactor feed pump, exchanging heat by a first raw material heat exchanger and a second heat exchanger, and then feeding the liquid-phase material into an alkylation reactor; and 5) exchanging heat of the alkylation reaction product through a raw material second heat exchanger, taking heat through a steam generator, and reducing pressure through a hydraulic turbine to enter a reaction product flash tank.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: and 5) flashing the alkylation reaction product in a reaction product flash tank to obtain non-condensable gas, cooling the non-condensable gas by a hot water heat exchanger and a cooler and then feeding the non-condensable gas into an absorbent feeding tank, feeding the gas discharged from the top of the absorbent feeding tank into a deethanizer, feeding the recovered ethane-rich gas into other devices, and feeding the condensate at the bottom of the deethanizer, which is rich in benzene, back to the product separation unit.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: the ethane-rich gas at the top of the ethane recovery tower in the step 6) can be directly used as a raw material of an ethylene cracking device.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: in step 5), the hydraulic turbine outlet pressure is 0.3MPag to 1.5MPag, preferably 0.4 to 0.7MPag, for driving the reactor feed pump, but also for driving other electrical consumers.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: the alkylation reactor is a liquid phase alkylation reactor, one or N alkylation reactors are connected in parallel, when N alkylation reactors are connected in parallel, the feeding of the alkylation reactor is divided into N liquid phase materials which respectively enter N reactors (or reaction bed layers), N is preferably equally divided, N is more than or equal to 1 and less than or equal to 10, and the number of N is determined according to the engineering design scale of the device for preparing ethylbenzene by the ethylene-containing dry gas-liquid phase method.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: the inlet temperature range of the liquid phase alkylation reactor is 150-250 ℃, the pressure range is 2.5-5 MPag, and the temperature rise range of the alkylation reactor is 5-60 ℃. Preferably, the inlet temperature of the alkylation reactor is 180-220 ℃, the pressure is 3.0-4.0 MPag, and the temperature rise of the alkylation reactor is 10-25 ℃. The molar ratio of the total benzene/the total ethylene fed into the alkylation reaction unit is 1.2-4.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: the ethane recovery tower has 5-50 layers of theoretical plates, the pressure at the top of the tower is 0.2-2.0 MPag, preferably 0.4-1.0 MPag, and the temperature of the absorbent entering the top of the tower is 15-40 ℃.
The invention relates to a process for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized by comprising the following steps: and (3) sending the reaction product from the alkylation reaction unit to a product separation unit, and separating to obtain an ethylbenzene product, polyethylbenzene, recycle benzene and the like. The product separation unit comprises a tail gas absorption tower, a benzene recovery tower, an ethylbenzene rectification tower, a propyl benzene tower, a polyethylbenzene tower, a non-aromatic tower, a transalkylation reactor and the like.
The invention also provides an application device of the process for producing ethylbenzene by using the ethylene-containing dry gas-liquid phase method, which comprises an ethylene-containing dry gas pretreatment unit, a propylene removal unit, a benzene drying unit, an alkylation reaction unit and a product separation unit, wherein the units are connected through pipelines, and the process is characterized in that: the ethylene-containing dry gas pretreatment unit comprises a water washing tower and a dry gas compressor in sequence; the propylene removal unit comprises a propylene absorption tower and a propylene desorption tower which are connected with each other through a pipeline in sequence; the benzene drying unit is a benzene dryer; the alkylation reaction unit comprises an ethylene absorption tower, an absorbent feeding tank, a raw material heat exchanger, an alkylation reactor, a steam generator, a product flash tank and a deethanizer, which are connected with each other through pipelines; the pipeline at the water washing tower part is connected with the lower part of the propylene absorption tower through a dry gas compressor; the outlet of the dry gas compressor is connected with the middle part of the propylene absorption tower; the top of the propylene absorption tower is connected with the lower part of the ethylene absorption tower;
the invention relates to a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized in that: the benzene dryer is connected with an absorbent feeding tank of the alkylation reaction unit;
the invention relates to a device for preparing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized in that: and a dryer is also arranged before the propylene-removed dry gas enters the ethylene absorption tower, and pipelines at the top of the propylene absorption tower respectively enter the ethylene absorption tower through the dryer.
The invention relates to a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized in that: the middle part of the bottom of the propylene absorption tower is connected with the feeding of an absorbent heat exchanger, the discharging of the absorbent heat exchanger is connected with the lower part of the propylene absorption tower, and the bottom of the propylene absorption tower is connected with the middle part of a propylene desorption tower; the bottom of the propylene desorption tower is connected with the top of the propylene absorption tower through an absorbent circulating pump.
The invention relates to a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized in that: the bottom of an ethylene absorption tower in the alkylation reaction unit is connected with the bottom of an alkylation reactor through a reactor feed pump; the top of the alkylation reactor enters a product flash tank through a hydraulic turbine, the top of the product flash tank enters an absorbent feeding tank through a flash gas heat exchanger, the top of the absorbent feeding tank is connected with the lower part of a deethanizer, and the bottom of the product flash tank is respectively communicated with an ethylene absorption tower and a product separation unit; the bottom of the absorbent feeding tank is communicated with the ethylene absorption tower through an absorbent booster pump.
The invention relates to a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized in that: the bottom of the ethylene absorption tower is connected with the bottom of the alkylation reactor through a reactor feed pump, a raw material first heat exchanger and a raw material second heat exchanger; the top of the alkylation reactor is connected with a product flash tank through a second raw material heat exchanger, a steam generator and a hydraulic turbine.
The invention relates to a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized in that: the bottom of the product flash tank is communicated with the first raw material heat exchanger and is divided into two paths, and one path is communicated with the product separation unit; the other path is communicated with an absorbent cooler through an absorbent feeding tank and an absorbent booster pump; the outlet of the absorbent cooler is communicated with the ethylene absorption tower.
The invention relates to a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized in that: the upper part and the bottom of the deethanizer are respectively communicated with a product separation unit; the top of the ethylene absorption tower is communicated with a product separation unit.
The invention relates to a device for producing ethylbenzene by an ethylene-containing dry gas-liquid phase method, which is further characterized in that: the absorbent circulating pump can be connected with the top of the propylene absorption tower through an absorbent heat exchanger and an absorbent buffer tank.
Compared with the prior art, the invention has the beneficial effects that:
1. the method comprises the steps of washing the raw material ethylene-containing dry gas with water, pressurizing by a compressor, cooling and separating liquid, wherein the pressure is increased to be beneficial to separating moisture in the gas from the gas phase, the gas phase after liquid separation is absorbed by a propylene absorption tower, most of moisture in the gas phase is dissolved in an absorbent, the moisture in the absorbent is separated out of the system in an absorbent buffer tank and a propylene desorption tower system, the moisture content in the top-tower propylene-removing dry gas is obviously reduced, and the propylene-removing dry gas can be directly fed into the ethylene absorption tower without a dryer to be absorbed and then used as the feed for alkylation reaction. If the operation fluctuation is considered, a dryer can be arranged before the dry gas enters the ethylene absorption tower for protection. The water content in the propylene-removed dry gas from the propylene-removing unit is not more than 20ppm, so that the requirement of most catalysts on the water content in the dry gas is not more than 100ppm, the active center of the catalyst is not influenced by the water content in the dry gas, and the activity and the service life of the catalyst are maximized.
2. The invention dissolves all the ethylene in the dry gas by means of proper pressurization and absorption and then liquid phase pressurization, and the ethylene is pressurized to the pressure required by the reaction by a pump after being dissolved, thereby greatly reducing the dosage of the circulating absorbent, reducing the size of equipment and pipelines and reducing the investment of devices. The economy of the device is improved.
3. The invention adopts liquid phase alkylation reaction to produce ethylbenzene, avoids direct contact between gas phase ethylene and the catalyst, and delays coking and inactivation of the catalyst. The liquid phase alkylation reaction temperature is controlled at 150-220 ℃, the occurrence of side reactions, particularly the generation of dimethylbenzene, is reduced, the content of dimethylbenzene in an ethylbenzene product is reduced, the conversion rate of ethylene is improved, and the yield of ethylbenzene is correspondingly increased.
4. The alkylation reactor is one or N parallel reactors, when N parallel reactors are connected, the feeding of the alkylation reactor needs to be divided into N liquid phase materials which respectively enter N reactors or reaction bed layers, N is more than or equal to 1 and less than or equal to 10, N is determined by the scale of ethylbenzene, the molar ratio of total benzene/total ethylene in the feeding of an alkylation reaction unit is 1.2-4, the benzene-olefin ratio in the feeding of each reactor is more than or equal to 15, the ethylene conversion rate and the selectivity are high, and the temperature rise of the reactors or the reaction bed layers is controllable.
5. The reaction part of the invention fully recycles the alkylation reaction heat, and the reaction part basically does not need external heat, compared with the process for preparing ethylbenzene by a gas phase method containing ethylene dry gas, the invention cancels facilities such as a circulating benzene heating furnace and the like, and greatly reduces the energy consumption of the device.
6. The alkylation reaction unit is provided with the flash tank, after the alkylation product is subjected to work and pressure reduction by the hydraulic turbine, most of noncondensable gas (CH 4, C2H6, trace H2, N2, CO2 and the like) dissolved in reaction materials is flashed out in the flash tank, so that the absorption capacity of the circulating absorption liquid to ethylene is increased, and the consumption of the circulating absorption liquid is reduced.
7. The alkylation reaction unit is provided with the ethane recovery tower, benzene, ethylbenzene and the like carried in the non-condensable gas of the flash tank are recovered and returned to the product separation unit, and can also be returned to the reaction feed to continuously participate in the reaction, and the ethane-rich gas at the top of the ethane recovery tower can be directly used as the raw material of the ethylene cracking device, so that the utilization rate of ethane in dry gas is improved.
8. The invention boosts the pressure before the raw material ethylene-containing dry gas enters the propylene absorption tower, and has better absorption effect at the same absorption temperature because the pressure is high, which is beneficial to gas absorption.
The present invention will be described in further detail with reference to the following drawings and detailed description, but the present invention is not limited to the scope of the present invention.
Drawings
FIG. 1 is a schematic view of a process flow of an apparatus for producing ethylbenzene by a dry gas-liquid phase method with ethylene according to the present invention, in which a compressor is provided in front of a propylene absorption tower;
FIG. 2 is a schematic view of the process flow of FIG. 1 with a dryer installed therein;
wherein the reference symbols shown are: 1-a water washing tower; 2-a dryer; a 3-propene absorption column; 4-an absorbent heat exchanger; a 5-propylene desorber; 6-a mixer; a 7-benzene dryer; 8-dry gas compressor; 9-an ethylene absorber column; 10-reactor feed pump; 11-feedstock first heat exchanger; 12-a feedstock second heat exchanger; 13-standby steam heater; 14-an alkylation reactor; 15-a steam generator; 16-a hydraulic turbine; 17-product flash tank; 18-flash gas heat exchanger; 19-an absorbent feed tank; 20-an absorbent booster pump; 21-an absorbent cooler; a 22-deethanizer; 23-product separation unit, 24-lean recycle absorption liquid, 25-absorbent buffer tank.
Detailed Description
The invention will be further explained with reference to the drawings.
As shown in the attached figure 1, the process and the device for producing the ethylbenzene by the ethylene-containing dry gas-liquid phase method comprise the following steps:
ethylene-containing dry gas from which acid gas is removed enters a water washing tower 1 from an upstream device, trace MDEA and other impurities carried in the dry gas are removed through water washing, the dry gas is compressed, boosted, cooled and separated by a dry gas compressor 8, a gas phase enters a propylene removal unit, and a separated liquid phase is discharged out of a system;
the ethylene-containing dry gas after liquid separation enters the middle part of a propylene absorption tower 3 of a propylene removal unit, and is in countercurrent contact with an absorbent entering from the top of the tower in the propylene absorption tower 3 to absorb propylene and heavy components in the dry gas; the dry gas of the propylene removed from the top of the propylene absorption tower 3 enters an alkylation reaction unit, the liquid phase material in the middle of the propylene absorption tower 3 is pumped by a pump and sent to an absorbent heat exchanger 4 to exchange heat with a high-temperature circulating absorbent from the bottom of the propylene desorption tower 5, and then enters the lower part of the propylene absorption tower 3, and the material at the bottom of the propylene absorption tower 3 is decompressed and sent to the propylene desorption tower 5. Pumping out materials at the bottom of the propylene desorption tower 5 serving as a poor circulation absorbent, sending the poor circulation absorbent into the absorbent heat exchanger 4 for heat exchange, cooling the poor circulation absorbent, then sending the poor circulation absorbent into the absorbent buffer tank 25, reducing the flow rate of the absorbent after entering the tank, settling the water in the absorbent in the tank and accumulating the water at the bottom of the tank, discharging the water out of the system through a water diversion bag, and sending the water-diverted circulation absorbent into the propylene absorption tower 3; the rich propylene gas at the top of the propylene desorption tower 5 is sent out of the device;
fresh benzene from outside the battery compartment is mixed with recycled benzene from the product separation unit 23 in the mixer 6, and then enters the benzene dryer 7 for dehydration, and the dehydrated mixed benzene is sent to the absorbent feed tank 19 of the alkylation reaction unit.
The dry depropylene gas from the top of a propylene absorption tower 3 of a depropylene unit enters the lower part of an ethylene absorption tower 9 of an alkylation reaction unit and is in countercurrent contact with lean cycle absorption liquid 24 entering from the top of the tower, absorption tail gas unabsorbed from the top of the ethylene absorption tower 9 is sent to a product separation unit 23 to recover benzene carried in the gas, rich cycle absorption liquid at the bottom of the tower is pressurized by a reactor feed pump 10, then enters an alkylation reactor 14 after passing through a raw material first heat exchanger 11 and a raw material second heat exchanger 12, the alkylation reaction product exchanges heat by the raw material second heat exchanger 12 and is heated by a steam generator 15, then is decompressed by a hydraulic turbine 16 and enters a product flash tank 17, the gas phase coming out of the top of the reaction product flash tank 17 enters a flash gas heat exchanger 18 to be cooled, the flash gas heat exchanger 18 can produce hot water by-production or is cooled by circulating water, then enters an absorbent feed tank 19 to be separated, and the uncondensed gas phase enters a deethanizer 22. The liquid phase material from the bottom of the product flash tank 17 exchanges heat with the first heat exchanger 11 of the raw material and then is divided into two streams, the first stream of the material enters an absorbent feeding tank 19, is mixed with the mixed benzene from the benzene drying unit, is pumped out by an absorbent booster pump 20, is cooled by an absorbent cooler 21 and then is sent to the top of the tower as the circulating absorption liquid 24 of the ethylene absorption tower; the other part is sent to a subsequent product separation unit 23 as a product; the absorbent from the product separation unit 23 enters the top of the deethanizer 22, and after the absorbent is in countercurrent contact with the absorption tail gas from the top of the ethylene absorption tower 9, the ethane-rich gas which is not absorbed is sent out from the top of the tower and is taken as the raw material of an ethane cracking device; the bottoms of the deethanizer 22 are sent to a product separation unit 23.
The reaction product from the alkylation reaction unit is separated in the product separation unit 23 to obtain products or intermediate products such as ethylbenzene, polyethylbenzene and recycle benzene.
In order to adapt to a larger-scale ethylbenzene production device, one or more parallel alkylation reactors 14 and corresponding matched systems such as heat exchange, pressure reduction, flash evaporation and the like can be added in an alkylation reaction unit;
the difference between the attached figure 2 and the attached figure 1 is that a dryer is arranged as a protective bed before the mixed dry gas enters the ethylene absorption tower 9, and the requirement of the catalyst on the water content in the dry gas can be still met when the upstream equipment fluctuates.
[ example 1 ] A method for producing a polycarbonate
A device for preparing ethylbenzene by catalyzing dry gas and liquid phases at a rate of 40 ten thousand tons/year adopts the flow of the figure 1.
Wherein:
a theoretical plate 24 layer of the propylene absorption tower, the absorption pressure of 0.9MPag and the absorption temperature of 15 ℃;
the ethylene absorption tower adopts a packed tower or a plate tower, the absorption pressure is 2.0MPag, and the absorption temperature is 40 ℃;
the molar ratio of total benzene/total ethylene fed to the alkylation reaction unit is 3.1;
an alkylation reactor: setting 2 units, one for one, and one for standby, wherein the reaction temperature is 205 ℃, and the pressure is 3.0MPag;
the outlet pressure of the hydraulic turbine is 0.6MPag;
the deethanizer employs 10 theoretical plates, and the overhead pressure is 0.55MPag.
The process conditions and feed data are shown in table 1.
TABLE 1 raw materials ethylene-containing Dry gas composition
The isolated product of this example is shown in table 2.
TABLE 2 Main product yields and compositions
| Propylene-rich gas | Ethane-rich gas | Ethylbenzene production | Polyethylbenzene | Non-aromatic | |
| Mass flow rate kg/h | 1163 | 5006 | 47619 | 4780 | 662 |
| H 2 | 60 | ||||
| N 2 | 376 | 6 | |||
| O 2 | 65 | ||||
| CO 2 | 1.6 | 188 | 42 | ||
| CH 4 | 1629 | 106 | |||
| C 2 H 4 | 82 | ||||
| C 2 H 6 | 195 | 2681 | 480 | ||
| C 3 H 6 | 744 | ||||
| C 3 H 8 | 19 | ||||
| Benzene and its derivatives | 16 | 13 | 28 | ||
| C4、C5 | 67 | ||||
| Ethylbenzene production | 47538 | ||||
| Polyethylbenzene | 5 | 15 | 451 |
According to calculation, in the embodiment, the ethylene conversion rate can reach more than 99.95%, and the ethylene recovery rate can reach more than 99.1%. Compared with the gas phase process with the same specification, the energy consumption of the device is reduced by about 50 percent.
While the embodiments of the present invention have been described in detail, it is to be understood that the present invention is not limited to the above embodiments and that various changes may be made without departing from the spirit and scope of the present invention by those skilled in the art, such as by providing pumps, air coolers, heat exchangers, and equal or unequal N liquid phase alkylation reaction feeds as required, for example, 1 or more ethylene absorption columns, for example, N liquid phase reactors, for example, parallel feeds or series-parallel feeds, and the like, within the scope of the present invention.
Claims (20)
1. The process for producing ethylbenzene by the ethylene-containing dry gas-liquid phase method comprises the following steps:
1) Firstly, washing an ethylene-containing dry gas raw material from the upstream to remove carried trace impurities, then entering a dry gas compressor, boosting the pressure by the dry gas compressor, and then sending a gas phase to a propylene removal unit;
2) The ethylene-containing dry gas after being boosted in the step 1) enters the middle part of a propylene absorption tower of a propylene removal unit and is in countercurrent contact with an absorbent entering from the top of the tower, the propylene-removed dry gas enters the ethylene absorption tower after coming out from the top of the propylene absorption tower, part of the absorbent is extracted from the middle section of the propylene absorption tower to exchange heat with a material from the bottom of a propylene desorption tower, and the heat is recovered and then returned to the lower section of the propylene absorption tower; feeding the material at the bottom of the propylene absorption tower to a propylene desorption tower; returning the material at the bottom of the propylene desorption tower after the removal of the propylene as a circulating absorbent to the top of the propylene absorption tower, and sending the propylene-rich gas at the top of the propylene desorption tower out of the device;
3) Fresh benzene enters a mixer, is mixed with circulating benzene from a product separation unit, enters a benzene dryer, is subjected to micro water removal in the benzene dryer, and is sent to an alkylation reaction unit;
4) And 2) introducing the depropylene dry gas from the top of the propylene absorption tower in the step 2) into the lower part of an ethylene absorption tower of an alkylation reaction unit, and making the depropylene dry gas contact with lean cycle absorption liquid entering from the top of the ethylene absorption tower in a countercurrent manner, conveying absorption tail gas from the top of the ethylene absorption tower to a product separation unit, and introducing the rich cycle absorption liquid from the bottom of the ethylene absorption tower into an alkylation reactor after boosting and heat exchange by using a pump.
5) Exchanging heat between a reaction product from an alkylation reactor and a reactor feeding material, reducing pressure, entering a reaction product flash tank, allowing a gas phase from the top of the reaction product flash tank to pass through a flash gas heat exchanger, then entering an absorbent feeding tank for liquid separation, allowing an uncondensed gas phase to enter a deethanizer, allowing a part of a liquid phase material from the bottom of the flash tank to be used as lean cycle absorption liquid of an ethylene absorption tower and be sent to the absorbent feeding tank, allowing a dried mixed benzene from the benzene drying unit in the step 3) to also enter the absorbent feeding tank, and then increasing the pressure of the mixed benzene and the benzene by an absorbent booster pump and sending the mixed benzene to the ethylene absorption tower; the other part is sent to a subsequent product separation unit;
6) The ethane-rich gas obtained by the separation at the top of the deethanizer is sent out of the device, and the components at the bottom of the deethanizer are sent to a subsequent product separation unit.
2. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: in the step 2), a dryer is arranged before the propylene-removed dry gas enters the ethylene absorption tower to remove trace moisture existing in the propylene-removed dry gas in a phase equilibrium manner, and the water content in the propylene-removed dry gas after drying is not more than 300ppm.
3. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: and 2) the absorbent is in countercurrent contact with the ethylene-containing dry gas in a propylene absorption tower to absorb propylene and heavy components in the ethylene-containing dry gas, and the absorbent contains one or more of benzene, ethylbenzene, methyl ethyl benzene and diethylbenzene.
4. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: the propylene absorption tower has 10-50 theoretical plates, tower top pressure of 0.6-4.5 MPag, absorption temperature of 5-60 deg.c and desorption temperature of 150-280 deg.c.
5. The process for producing ethylbenzene according to claim 1, wherein: : the outlet pressure of the dry gas compressor in the step 1) is 1.2-3.0 MPag.
6. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: and 4) the light component gas which is not absorbed at the top of the ethylene absorption tower enters a tail gas absorption tower of the product separation unit, after being absorbed by the heavy components such as ethylbenzene, polyethylbenzene or propylbenzene, methane and hydrogen at the top of the tower are sent to a fuel gas pipe network or other devices to recover hydrogen, and the absorbed liquid is sent to the product separation unit to recover benzene therein.
7. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: and 4) pressurizing the liquid-phase material from the bottom of the ethylene absorption tower by a reactor feed pump, exchanging heat by the first raw material heat exchanger and the second heat exchanger, and then feeding the liquid-phase material into an alkylation reactor.
8. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: and 5) exchanging heat of the alkylation reaction product through a raw material second heat exchanger, taking heat through a steam generator, and reducing pressure through a hydraulic turbine to enter a reaction product flash tank.
9. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: and 5) flashing noncondensable gas from the alkylation reaction product in a reaction product flash tank, cooling the noncondensable gas by a hot water heat exchanger and a cooler, feeding the noncondensable gas into an absorbent feeding tank, feeding the gas discharged from the top of the absorbent feeding tank into a deethanizer, feeding the recovered ethane-rich gas into other devices, and returning the condensate at the bottom of the deethanizer, which is rich in benzene, to a product separation unit.
10. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: in step 5), the outlet pressure of the hydraulic turbine is between 0.3MPag and 1.5MPag.
11. The process for producing ethylbenzene according to claim 1, wherein: the alkylation reactor is a liquid phase alkylation reactor, one or N alkylation reactors are connected in parallel, when N alkylation reactors are connected in parallel, the feeding of the alkylation reactor is divided into N liquid phase materials which respectively enter N reactors (or reaction bed layers), N is preferably equally divided, N is more than or equal to 1 and less than or equal to 10, and the number of N is determined according to the engineering design scale of the device for preparing ethylbenzene by the ethylene-containing dry gas-liquid phase method.
12. The process for producing ethylbenzene according to claim 1, wherein: the inlet temperature range of the liquid phase alkylation reactor is 150-250 ℃, the pressure range is 2.5-5 MPag, and the temperature rise range of the alkylation reactor is 5-60 ℃.
13. The process for producing ethylbenzene by the dry gas-liquid phase method containing ethylene according to claim 1, wherein: the ethane recovery tower has 5-50 layers of theoretical plates, the pressure at the top of the tower is 0.2-2.0 MPag, and the temperature of the absorbent entering the top of the tower is 15-40 ℃.
14. The device for producing ethylbenzene by the ethylene-containing dry gas-liquid phase method according to the process of claims 1-13, which comprises an ethylene-containing dry gas pretreatment unit, a propylene removal unit, a benzene drying unit, an alkylation reaction unit and a product separation unit, wherein the units are connected through pipelines, and is characterized in that: the ethylene-containing dry gas pretreatment unit comprises a water washing tower and a dry gas compressor in sequence; the propylene removal unit comprises a propylene absorption tower and a propylene desorption tower which are connected through a pipeline in sequence; the benzene drying unit is a benzene dryer; the alkylation reaction unit comprises an ethylene absorption tower, an absorbent feeding tank, a raw material heat exchanger, an alkylation reactor, a steam generator, a product flash tank and a deethanizer, which are connected with each other through pipelines; the pipeline at the water washing tower part is connected with the lower part of the propylene absorption tower through a dry gas compressor; the outlet of the dry gas compressor is connected with the middle part of the propylene absorption tower; the top of the propylene absorption tower is connected with the lower part of the ethylene absorption tower.
15. The apparatus for producing ethylbenzene according to claim 14, wherein: the benzene dryer is connected to the absorbent feed tank of the alkylation reaction unit.
16. The apparatus for producing ethylbenzene by dry gas-liquid phase process with ethylene according to claim 14, wherein: and a dryer is also arranged before the depropylene dry gas enters the ethylene absorption tower, and pipelines at the top of the propylene absorption tower respectively enter the ethylene absorption tower through the dryer.
17. The apparatus for producing ethylbenzene according to claim 14, wherein: the middle part of the bottom of the propylene absorption tower is connected with the feeding of an absorbent heat exchanger, the discharging of the absorbent heat exchanger is connected with the lower part of the propylene absorption tower, and the bottom of the propylene absorption tower is connected with the middle part of a propylene desorption tower; the bottom of the propylene desorption tower is connected with the top of the propylene absorption tower through an absorbent circulating pump.
18. The apparatus for producing ethylbenzene according to claim 14, wherein: the bottom of an ethylene absorption tower in the alkylation reaction unit is connected with the bottom of an alkylation reactor through a reactor feed pump; the top of the alkylation reactor enters a product flash tank through a hydraulic turbine, the top of the product flash tank enters an absorbent feeding tank through a flash gas heat exchanger, the top of the absorbent feeding tank is connected with the lower part of a deethanizer, and the bottom of the product flash tank is respectively communicated with an ethylene absorption tower and a product separation unit; the bottom of the absorbent feeding tank is communicated with the ethylene absorption tower through an absorbent booster pump.
19. The apparatus for producing ethylbenzene by dry gas-liquid phase process with ethylene according to claim 14, wherein: the bottom of the ethylene absorption tower is connected with the bottom of the alkylation reactor through a reactor feed pump, a raw material first heat exchanger and a raw material second heat exchanger; the top of the alkylation reactor is connected with a product flash tank through a second raw material heat exchanger, a steam generator and a hydraulic turbine.
20. The apparatus for producing ethylbenzene according to claim 14, wherein: the bottom of the product flash tank is communicated with the first raw material heat exchanger and is divided into two paths, and one path is communicated with the product separation unit; the other path is communicated with an absorbent cooler through an absorbent feeding tank and an absorbent booster pump; the outlet of the absorbent cooler is communicated with the ethylene absorption tower.
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| US20040167371A1 (en) * | 2003-02-25 | 2004-08-26 | Pohl Stephen L. | Process for the production of alkylbenzene |
| CN107827692A (en) * | 2017-04-28 | 2018-03-23 | 常州瑞华化工工程技术有限公司 | A kind of method that ethylbenzene is produced with high concentration ethylene gas |
| CN114669245A (en) * | 2022-04-08 | 2022-06-28 | 中石化广州工程有限公司 | Device for preparing ethylbenzene by ethylene-containing dry gas-liquid phase method |
| CN114671732A (en) * | 2022-04-07 | 2022-06-28 | 中石化广州工程有限公司 | Process for preparing ethylbenzene by ethylene-containing dry gas-liquid phase method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040167371A1 (en) * | 2003-02-25 | 2004-08-26 | Pohl Stephen L. | Process for the production of alkylbenzene |
| CN107827692A (en) * | 2017-04-28 | 2018-03-23 | 常州瑞华化工工程技术有限公司 | A kind of method that ethylbenzene is produced with high concentration ethylene gas |
| CN114671732A (en) * | 2022-04-07 | 2022-06-28 | 中石化广州工程有限公司 | Process for preparing ethylbenzene by ethylene-containing dry gas-liquid phase method |
| CN114669245A (en) * | 2022-04-08 | 2022-06-28 | 中石化广州工程有限公司 | Device for preparing ethylbenzene by ethylene-containing dry gas-liquid phase method |
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