WO2015184677A1 - 工业合成气高压羰化生产草酸二甲酯并加氢制乙二醇的工艺和装置系统 - Google Patents
工业合成气高压羰化生产草酸二甲酯并加氢制乙二醇的工艺和装置系统 Download PDFInfo
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- C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
- C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
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- C07C31/18—Polyhydroxylic acyclic alcohols
- C07C31/20—Dihydroxylic alcohols
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- C07C69/34—Esters of acyclic saturated polycarboxylic acids having an esterified carboxyl group bound to an acyclic carbon atom
- C07C69/36—Oxalic acid esters
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Definitions
- the invention relates to a process and a device system for industrial synthesis gas to produce ethylene glycol, in particular to a process for high-pressure carbonylation of industrial synthesis gas to produce dimethyl oxalate and hydrogenation to ethylene glycol, and a device system thereof.
- Ethylene glycol is a versatile chemical used in a variety of production areas such as polyester (PET), antifreeze, ethanolamine and explosives. It is used as a solvent, lubricant and plasticizer.
- PET polyester polyester
- the use of diols in the PET polyester industry is close to 95%.
- ethylene glycol production in the industry mainly adopts a route in which petroleum ethylene is subjected to gas phase oxidation to obtain ethylene oxime, and then liquid phase catalytic hydration to ethylene glycol.
- the world's ethylene-based ethylene glycol industry chain is facing tremendous pressure. Therefore, the use of syngas to ethylene glycol technology has attracted more and more attention due to its low production cost.
- the tubular-type reactor is mainly used in the process of coal-to-ethylene glycol.
- the heat transfer efficiency of the reaction heat is low, the utilization coefficient of the catalyst and the packing coefficient are low, thereby affecting the reactor production capacity.
- Patent Publication No. CN101462961
- the process includes the process of synthesizing dimethyl oxalate and dimethyl carbonate from CO and methyl nitrite, and separating the carbonate by distillation.
- the reactor adopts a tubular reactor, and the exhaust gas and waste liquid generated during the reaction process are not recycled and reused, and the energy consumption of the device is high, which cannot meet the increasing environmental protection needs of the country.
- Patent discloses a method and a device for co-production of dimethyl carbonate and dimethyl oxalate, the patent uses two carbonylation reactors, the first is a dimethyl carbonate synthesis reactor, the second It is a reactor of dimethyl oxalate. After the reaction of methyl nitrite is formed, it enters two reactors to produce dimethyl carbonate and dimethyl oxalate respectively, and then the product is separated and purified. From the perspective of process design, its essence It is only the simple accumulation of the two types of reactors, which can not truly realize the practical significance of DMO co-production DMC in the same device.
- Patent CN201210531022.1 discloses a method of concentrating the produced nitric acid and then reacting it with a portion of the NO-containing recycle gas to produce NO 2 and replenishing it back to the methyl nitrite regeneration reactor.
- the NO-containing recycle gas also contains a large amount of gases such as methyl nitrite and methanol. These gases also react with concentrated nitric acid, and the products are complicated, which affects the performance of the device.
- the coal-to-ethylene glycol process mainly has low catalyst utilization rate and low catalyst loading coefficient.
- the valuable gas in the device cannot be fully utilized, but the environment is polluted, and the heat of the device system cannot be fully utilized, thereby causing social and social
- the economic benefits are not satisfactory.
- the object of the present invention is to solve the problems of low utilization rate of raw materials, high production cost, low catalyst utilization rate, low packing factor, excessive equipment investment, single series equipment cannot adapt to large-scale equipment, and high system consumption.
- the use of the device cannot meet the requirements of the country for increasingly industrial environments, and provides a process and a device system for improving the production capacity of a single series of devices, exhaust gas treatment, by-product recovery, and comprehensive utilization of raw materials.
- the invention is achieved by the following technical solutions:
- An apparatus system for high-pressure carbonylation of industrial syngas to produce dimethyl oxalate and hydrogenation to ethylene glycol comprising a carbonylation reaction system, an esterification reaction system, a gas-and-gassing and waste acid coupling recovery system, and a hydrogenation reaction system;
- the carbonylation reaction system comprises a carbonylation reactor, a first gas-liquid separator, a methanol scrubber, a methanol condensate column and a DMO condensate column;
- the carbonylation reactor is provided with a top feed port and a bottom discharge port a bottom refrigerant inlet and a top refrigerant outlet;
- the first gas-liquid separator is provided with a feed port, a gas outlet, and a liquid outlet;
- the methanol scrubber is provided with an upper feed port, a lower feed port, a top outlet, and a bottom An outlet of the methanol, an upper feed port, a lower feed port, a top outlet, and a bottom
- the purge gas and waste acid coupling recovery system comprises a nitric acid concentration tower, a NO recovery tower, and a MN recovery tower And a pressure swing adsorption tank;
- the nitric acid concentration tower is provided with a middle feed port, a top outlet, and a bottom outlet;
- the NO recovery tower is provided with a top feed port, a middle feed port, a bottom feed port, a top outlet, and a bottom portion
- the MN recovery tower is provided with an upper feed port, a lower feed port, a top outlet and a bottom outlet;
- the pressure swing adsorption tank is provided with a feed port, a recovery gas outlet and an exhaust gas outlet;
- the system comprises a hydrogenation cycle compressor, a hydrogenation reactor, a second gas-liquid separator, a membrane separator, a methanol separation column, a light component refined column and an ethylene glycol product column;
- the hydrogenation cycle compressor includes an inlet And an outlet;
- the hydrogenation reactor is provided with
- the light component fine crucible tower is provided with a lower feed port, a top outlet and a bottom outlet;
- the ethylene glycol product tower is provided with a lower feed port, a top outlet, an upper outlet and a bottom outlet;
- the carbonylation reactor The top feed port is connected to the CO raw material pipe and the N 2 raw material pipe via a pipeline;
- the bottom discharge port of the carbonylation reactor is connected to the feed port of the first gas-liquid separator via a pipeline;
- the first gas a gas outlet of the liquid separator is connected to a lower feed port of the methanol scrubber;
- a liquid outlet of the first gas-liquid separator is connected to an upper feed port of the methanol streamer;
- the top outlet of the methanol scrubber is provided with a branch outlet A and a branch outlet B, and the branch outlet A is connected to a lower feed port of the esterification reaction tower via a line, the branch outlet B and the bottom feed port of the NO recovery tower Connected via a pipeline;
- the branch outlet E is connected to the upper feed port of the esterification reaction tower via a line, and the branch outlet F and the upper portion of the MN recovery tower are fed.
- the bottom outlet of the methanol recovery tower is connected to the middle feed port of the nitric acid concentration column via a pipeline; the top outlet of the nitric acid concentration column is a waste liquid discharge port; the bottom outlet of the nitric acid concentration tower a middle feed port of the NO recovery column is connected via a pipeline; a top outlet of the NO recovery column is connected to a lower feed port of the MN recovery column; a bottom outlet of the NO recovery column and the methanol a middle and lower feed port of the recovery tower is connected by a pipeline; a top outlet of the MN recovery tower is connected to a feed port of the pressure swing adsorption tank via a pipeline; a bottom outlet of the MN recovery tower and the esterification reaction tower
- the upper feed port is connected by a pipeline; the recovery gas outlet of the pressure swing adsorption tank is
- a dehydration tower is connected outside the carbonylation reactor; the dehydration tower is provided with a feed port and a dry gas outlet; a top outlet of the esterification reaction column and a recovery gas outlet of the pressure swing adsorption tank are connected to a feed port of the dehydration column via a line; a dry gas outlet of the dehydration column and a top feed of the carbonation reactor The mouth is connected by a pipeline.
- the dehydration column is composed of two molecular sieve dryers A and molecular sieve dryers B which are alternately operated and regenerated; molecular sieve dryer A and molecular sieve dryer B are filled with adsorbent; the adsorbent is selected from 3A molecular sieve, 4A molecular sieve, 5A Molecular sieves, 9A molecular sieves and calcium oxide.
- the bottom discharge port of the carbonylation reactor is connected with an outlet heat exchanger I; the outlet heat exchanger I is provided with a cold stream inlet, a cold stream outlet, a hot material inlet and a hot stream outlet; the CO raw material pipeline, a drying gas outlet of the N 2 raw material pipeline and the dehydration tower is connected to the cold heat exchanger inlet of the outlet heat exchanger I; a cold stream outlet of the outlet heat exchanger I and a top feed port of the carbonation reactor a pipeline connection; a bottom discharge port of the carbonylation reactor is connected to a hot stream inlet of the outlet heat exchanger I; a hot stream outlet of the outlet heat exchanger I and the first gas-liquid separator
- the feed port is connected by a pipeline.
- the steaming reactor is externally connected with a steam drum I; the steam drum I is provided with a refrigerant inlet, a refrigerant outlet, a vapor-liquid mixture inlet and a steam outlet; and the refrigerant inlet of the steam drum I and the refrigerant raw material pipeline are connected by a pipeline;
- the refrigerant outlet of the steam drum I is connected to the bottom refrigerant inlet of the carbonylation reactor via a pipeline;
- the top refrigerant outlet of the carbonylation reactor is connected to the vapor-liquid mixture inlet of the steam drum I via a pipeline;
- the steam outlet of the steam drum I is connected to the outer steam recovery system via a pipeline.
- a carbonylation cycle compressor is connected between the branch outlet A of the methanol scrubber and the lower feed port of the esterification reaction tower; the carbonylation cycle compressor is provided with an inlet and an outlet; The inlet of the carbonylation cycle compressor is connected by a pipeline; the outlet of the carbonylation cycle compressor is connected to a lower feed port of the esterification reaction column via a pipeline.
- a compressor is connected between a top outlet of the NO recovery tower and a bottom feed inlet of the MN recovery tower; the compressor is provided with an inlet and an outlet; a top outlet of the NO recovery tower is connected to the compressor The inlet is connected via a pipeline; the outlet of the compressor is connected to the bottom feed port of the MN recovery tower via a pipeline.
- the bottom discharge port of the hydrogenation reactor is connected with an outlet heat exchanger ⁇ ; the outlet heat exchanger II is provided with a cold stream inlet, a cold stream outlet, a hot material inlet and a hot stream outlet; a bottom outlet, a recovery gas outlet of the membrane separator, and an outlet of the hydrogenation cycle compressor connected to a cold stream inlet of the outlet heat exchanger II; a cold stream outlet of the outlet heat exchanger II Reversing with the hydrogenation
- the top feed port of the reactor is connected by a pipeline; the bottom discharge port of the hydrogenation reactor and the outlet heat exchanger
- the hot stream inlet of II is connected via a line; the hot stream outlet of the outlet heat exchanger II is connected to the feed port of the second gas-liquid separator via a line.
- a top feed inlet of the hydrogenation reactor is connected with a starter heater; the starter heater is provided with a feed port and a discharge port; a cold stream outlet of the outlet heat exchanger II and the start heater
- the feed port is connected by a pipeline; the discharge port of the start heater is connected to the top feed port of the hydrogenation reactor via a pipeline.
- the steam reactor is connected with a steam drum II; the steam drum II is provided with a refrigerant inlet, a refrigerant outlet, a vapor-liquid mixture inlet and a steam outlet; and the refrigerant inlet of the steam drum II and the refrigerant raw material pipeline are connected by a pipeline;
- the refrigerant outlet of the steam drum II is connected to the bottom refrigerant inlet of the hydrogenation reactor via a pipeline;
- the top refrigerant outlet of the hydrogenation reactor is connected to the vapor-liquid mixture inlet of the steam drum II via a pipeline;
- the steam outlet of the steam drum II is connected to the outer steam recovery system via a pipeline.
- the second gas-liquid separator comprises a high-pressure gas-liquid separator and a low-pressure gas-liquid separator; the high-pressure gas-liquid separator is provided with a feed port, a gas outlet and a liquid outlet; and the low-pressure gas-liquid separator is provided with a feed port, a gas outlet and a liquid outlet; the hot stream outlet of the outlet heat exchanger II is connected to a feed port of the high-pressure gas-liquid separator; the gas outlet of the high-pressure gas-liquid separator is provided with a branch outlet K and branch outlet L, the branch outlet K is connected to the inlet of the hydrogenation cycle compressor via a line, and the branch outlet L is connected to the inlet of the low-pressure gas-liquid separator via a pipeline; the high-pressure gas-liquid separator a liquid outlet is connected to a middle feed port of the methanol separation column via a pipeline; a gas outlet of the low pressure gas-liquid separator is connected to a feed port of the membrane separator via a pipeline; and a liquid
- a methanol absorption tank is disposed in front of the feed port of the membrane separator; the methanol absorption tank is provided with a feed port and a purge gas outlet; the gas outlet of the low pressure gas-liquid separator and the top of the methanol separation column are not
- the condensate outlet is connected to the feed port of the methanol absorption tank via a pipeline; the purge gas outlet of the methanol absorption tank is connected to the feed port of the membrane separator via a pipeline.
- the carbonylation reactor is a plate reactor, a tubular reactor or a tubular-plate composite reactor.
- the carbonylation reactor is a plate type fixed bed carbonylation reactor.
- the center of the plate type fixed bed carbonylation reactor is provided with a plate group fixing cavity, and the plate group a fixed plate is provided with a plate group, the plate group fixing cavity is further provided with a bottom inlet and a top outlet;
- a catalyst bed is arranged between the outer wall of the plate group fixing cavity and the inner wall of the plate fixed bed carbonation reactor a catalyst bed is filled with a carbonylation catalyst, the catalyst bed is further provided with a top inlet and a bottom outlet;
- the plate fixed bed carbonylation reactor a bottom refrigerant inlet is connected to the bottom inlet of the fixed portion of the plate group via a pipeline, and a bottom outlet of the catalyst bed is connected to a bottom discharge port of the plate fixed bed carbonylation reactor via a pipeline;
- the top feed port of the plate fixed bed carbonylation reactor is connected to the top in
- the esterification reaction column is a packed column.
- the esterification reaction column is a tray-filler mixing tower having both a tray portion and a packed portion of the filler.
- the methanol scrubbing tower, the methanol quenching tower, the methanol recovery tower, the NO recovery tower, the MN recovery tower, the DMO fine crucible tower and the nitric acid concentration tower are packed towers, tray towers or bubble columns.
- the filler packed in the packed tower is a random packing or an efficient structured packing; the random packing is in the shape of a saddle shape, a Raschig ring, a Pall ring, a wheel shape, a saddle ring, a spherical shape or a column shape.
- the high efficiency structured packing is a corrugated packing, a grid packing or a pulse packing.
- the hydrogenation reactor is more preferably a plate reactor, a tubular reactor or a tubular-plate composite reactor, and the hydrogenation reactor is a plate type fixed bed hydrogenation reactor.
- the center of the plate-type fixed-bed hydrogenation reactor is provided with a plate group fixing cavity, and the plate group fixing cavity is provided with a plate group, and the plate group fixing cavity is further provided with a bottom inlet and a top a catalyst bed is disposed between the outer wall of the fixed portion of the plate group and the inner wall of the plate-type fixed bed hydrogenation reactor; the catalyst bed is filled with a hydrogenation catalyst, and the catalyst bed is further provided a top inlet and a bottom outlet; at a bottom of the plate-type fixed-bed hydrogenation reactor, a bottom refrigerant inlet of the plate-type fixed-bed hydrogenation reactor is connected to a bottom inlet of the plate-set fixed chamber via a line, the catalyst a bottom outlet of the bed is connected to the bottom discharge port of the plate-type fixed bed hydrogenation reactor via a pipeline; in the plate-type fixed bed hydrogenation reaction At the top of the apparatus, a top feed port of the plate-type fixed bed hydrogenation reactor is connected to a top inlet of the catalyst bed
- the membrane separator is composed of 1 to 100 hollow fiber membrane modules connected in parallel or in series.
- a process for high-pressure carbonylation of industrial synthesis gas to produce dimethyl oxalate and hydrogenation to ethylene glycol, to produce methyl nitrite by esterification reaction using industrial grade NO, 0 2 and methanol as raw materials, and then use industrial grade CO The carbonylation reaction with methyl nitrite produces carbonylation products mainly of dimethyl oxalate and dimethyl carbonate.
- the carbonylation product is separated to obtain dimethyl carbonate product, and dimethyl oxalate is hydrogenated to form ethylene.
- the alcohol product; and the waste acid of the esterification reaction and the purge gas of the carbonylation reaction are recycled by the coupled recovery treatment.
- the process for producing dimethyl oxalate by high pressure carbonylation of an industrial syngas and hydrogenating it to ethylene glycol comprises the following steps:
- esterification reaction (1) introducing esterification reaction of industrial grade NO, 0 2 and methanol into the esterification reaction column; esterification reaction tower top methyl nitrite mixed gas is introduced into the carbonylation reactor for carbonylation reaction; esterification reaction The acid alcohol solution of the Tata kettle is partially refluxed to the esterification reaction column, and partially passed to the methanol recovery column; the methanol recovered from the top of the methanol recovery column is partially recycled to the esterification reaction column for recycling, and the rest is taken to the MN recovery column as a washing liquid; The waste acid in the Tata kettle enters the nitric acid concentration tower for concentration treatment;
- the carbonylation product enters the first gas-liquid separator to be separated from the gas-liquid separation, the gas phase enters the methanol scrubber, and the liquid phase enters the methanol-fine column; the gas phase component of the methanol scrubber is partially recycled to the esterification column, partly as The gas is discharged into the NO recovery tower for recovery; the liquid phase component of the methanol scrubbing tower is sent to the methanol fine column for fine separation; the mixture of methanol and methyl nitrite recovered from the top of the methanol refined column is recycled to the esterification reaction.
- the tower is reused, and the heavy components of the tower are entered into the DMO fine tower; The DMO product is obtained from the top of the DMO fine column, and the dimethyl oxalate component of the column is charged into the hydrogenation reactor for hydrogenation reaction;
- the spent acid from the methanol recovery tower is concentrated in a nitric acid concentration column to a concentration of 10 to 68% by weight of nitric acid, and then recycled to the NO recovery tower; in the NO recovery tower, concentrated nitric acid, methanol and a washing tower from the methanol washing tower Gas generation esterification regeneration reaction; NO recovery tower overhead gas phase light component enters MN recovery tower, and methanol-containing nitric acid waste liquid generated in the tower reactor is recycled to the methanol recovery tower for further recovery treatment; in the MN recovery tower, the gas phase feed is passed through After washing the recovered methanol, it enters the pressure swing adsorption tank, and the alcohol solution containing methyl nitrite in the MN recovery tower is recycled to the esterification reaction tower; the CO 2 separated from the pressure swing adsorption tank is discharged to the outside treatment, and the recovered N 2 and The CO purification gas enters the carbonylation reactor for recycling;
- the hydrogenation product enters the second gas-liquid separator to be gas-liquid separated, and the gas phase is recycled to the hydrogenation reactor after being pressurized by the hydrogenation cycle compressor, and partially enters the membrane separator and is returned to the hydrogenation after being recovered.
- the reactor is recycled, and the liquid phase is separated into an ethylene glycol product column to obtain an ethylene glycol product.
- the decarbonylation reactor is connected with a dehydration tower; the gas phase recovered by the pressure swing adsorption tank and the methyl nitrite mixture from the top of the esterification reaction tower are removed by the dehydration tower, The carbonylation reactor is further introduced into the carbonylation reactor.
- the dehydration column is composed of two molecular sieve dryers A and molecular sieve dryers B which are alternately operated and regenerated; the molecular sieve dryer A and the molecular sieve dryer B are filled with an adsorbent; the adsorbent is selected from the group consisting of 3A molecular sieves, 4A molecular sieve, 5A molecular sieve, 9A molecular sieve and calcium oxide.
- the molecular sieve dryer A and the molecular sieve dryer B have an operating temperature of 40 to 260 ° C and a pressure of 1 to 10 MPa. Unless otherwise stated, all pressures in the present invention refer to gauge pressure.
- the drying gas is obtained by a dehydration tower, and the moisture content in the drying gas is 0.1 to 100 ppm.
- the carbonylation reactor is externally connected with an outlet heat exchanger I; industrial grade CO, N 2 and from The drying gas of the dehydration tower is used as a raw material for the carbonylation reaction, and is exchanged with the carbonylation reaction product from the carbonylation reactor through the outlet heat exchanger I to be subjected to a carbonylation reaction.
- a portion of the gas phase component from the top of the methanol scrubber is pressurized by a carbonylation recycler and then passed to the esterification column.
- the top gas phase light component of the NO recovery tower is compressed and pressurized by a compressor and then enters the MN recovery tower.
- the hydrogenation reactor is externally connected with an outlet heat exchanger ⁇ ; a dimethyl oxalate component from a DMO condensate column, industrial hydrogen and recycle gas from a pressurized recycle compressor, and recovery from a membrane separator.
- the gas is used as a hydrogenation reaction raw material, and is exchanged with the hydrogenation product from the hydrogenation reactor through the outlet heat exchanger, and then enters the hydrogenation reactor for hydrogenation reaction.
- the liquid phase separated by the second gas-liquid separator first enters the methanol separation column; the non-condensed gas recovered at the top of the methanol separation column enters the membrane separator, and the liquid phase light component such as methanol recovered at the top of the methanol separation column Partially entering the upper part of the methanol scrubbing tower as a washing liquid, and partially entering the NO recovery tower; the liquid phase heavy component of the methanol separation tower bottom tank enters the light component fine crucible tower for further separation and purification; the light component fine tower top light component Entering the extra-regional alcohol recovery unit for recycling treatment; the light component refined ⁇ Tata kettle heavy component enters the ethylene glycol product tower; the ethylene glycol product tower top light component enters the boundary 1, 2-BDO recovery treatment device is further recycled The heavy component of the glycol product Tata kettle enters the out-of-band recovery treatment device for subsequent treatment, and the upper side line of the ethylene glycol product tower leads to the ethylene glycol product.
- the second gas-liquid separator comprises a high-pressure gas-liquid separator and a low-pressure gas-liquid separator; a gas phase separated by a high-pressure gas-liquid separator enters the hydrogenation cycle compressor, and partially enters the low-pressure gas a liquid separator; a liquid phase separated by the high-pressure gas-liquid separator enters the methanol separation column; a gas phase separated by the low-pressure gas-liquid separator enters the membrane separator, and the liquid separated by the low-pressure gas-liquid separator The phase enters the methanol separation column.
- 0.1 to 10% of the gas phase separated by the high-pressure gas-liquid separator enters the low-pressure gas-liquid separator.
- the gas phase separated by the low pressure gas-liquid separator and the non-condensable gas from the top of the methanol separation column are absorbed by the methanol absorption tank and then enter the membrane separator.
- the carbonylation reactor is a plate reactor, a tubular reactor or a tubular-plate composite reactor. More preferably, the carbonylation plate reactor is a plate type fixed bed carbonylation reactor.
- the center of the plate type fixed bed carbonylation reactor is provided with a plate group fixing cavity, and the plate piece group is provided with a plate group in the fixing cavity; the plate group fixing cavity outer wall to the plate type fixed bed carbonyl a catalyst bed is disposed between the inner walls of the reactor; the catalyst bed is filled with a carbonylation catalyst; after the carbonylation feed reaches the catalyst bed inlet temperature, the catalyst is introduced from the top of the plate-type fixed bed carbonylation reactor.
- the carbonylation reaction takes place in the bed; the refrigerant introduced from the outside enters the plate group fixed cavity from the bottom of the plate-type fixed bed carbonylation reactor, and is taken out from the top of the plate-type fixed-bed carbonylation reactor, and the heat exchange is carried out in the countercurrent process.
- the plate type fixed bed carbonylation reactor is connected with a steam drum I; the refrigerant introduced from the outside enters the steam drum I, and the refrigerant in the steam drum I enters the plate group fixed cavity of the plate type fixed bed carbonylation reactor.
- the heat exchange with the catalyst bed removes the heat of reaction; the heated refrigerant is a vapor-liquid mixture, enters the steam drum I for gas-liquid separation, and the generated low-pressure saturated steam enters the extra-low pressure steam recovery system for recycling.
- the carbonylation catalyst is a commercially available catalyst of Shanghai Wuzheng Engineering Technology Co., Ltd., and the catalyst brand number is DM0-0701T.
- the esterification reaction column is a packed column; preferably, the esterification reaction column is a tray-filler mixing tower having both a tray portion and a packed portion of the filler.
- the number of theoretical plates of the esterification reaction column is 20 to 50 pieces. The order of the number of the trays is set to be the first tray, and then sequentially arranged to the bottom of the tower.
- the 0 2 points 2 to 8 channels are respectively fed from the 16th to 50th trays; the NO and the overhead gas phase light group from the methanol scrubber Distilled from the 18th to 50th trays; the fresh methanol, the recovered methanol from the top of the methanol recovery tower, the methanol and nitrite mixture recovered from the top of the methanol refinery tower, and the MN recovery tower
- the methanol solution containing methyl nitrite in the kettle is fed from the first to fifth trays; the refluxing material in the esterification reaction tray is fed from the 10th to 25th trays.
- the molar ratio of 0 2 , NO and methanol in the esterification reaction column is 0.01 ⁇ 0.8: 0.1 ⁇ 3.2: 0. 8 ⁇ 50.
- the temperature of the top of the esterification reaction column is 30 to 80 ° C
- the temperature of the column is 50 to 200 ° C
- the temperature of the reaction zone is 50 to 160 ° C
- the reaction pressure is 0.5 to 10 MPa.
- the methanol recovery tower, the methanol scrubber, the methanol condensate tower, the nitric acid concentration tower, the NO recovery tower, the MN recovery tower, and the DMO fine condensate tower are packed towers, tray towers or bubble columns.
- the filler packed in the packed tower is a random packing or an efficient structured packing; the random packing is in the shape of a saddle shape, a Raschig ring, a Pall ring, a wheel shape, a saddle ring, a spherical shape or a column shape.
- the high efficiency structured packing is a corrugated packing, a grid packing or a pulse packing.
- the number of theoretical plates of the methanol recovery column is 5 to 50, the temperature at the top of the column is 40 to 150 ° C, the temperature of the column is 60 to 230 ° C, and the pressure at the top of the column is 0.01 to 2.0 MPa.
- the reflux ratio of the top component of the methanol recovery column is from 0.1 to 3.0.
- the proportion of the portion recycled to the esterification reaction column is 10 to 90 wt%.
- the number of theoretical plates of the methanol scrubber is 10 to 50, the temperature at the top of the column is 15 to 70 ° C, the temperature in the column is 10 to 100 ° C, and the pressure at the top of the column is 0.9 to 10 MPa.
- the proportion of the purge gas is 0.05 to 5 v%.
- the methanol condensate tower is an extractive condensate tower, the number of theoretical trays is 10 to 60, the temperature at the top of the column is 50 to 150 ° C, the temperature of the column is 130 to 250 ° C, and the pressure at the top of the column is 0.01. ⁇ 0.5MPa.
- the number of theoretical plates of the nitric acid concentration column is 1 to 30 pieces, the temperature at the top of the column is 30 to 110 ° C, the temperature of the column is 60 to 160 ° C, and the pressure at the top of the column is 0.01 to 0.3 MPa.
- the reflux ratio of the overhead light component of the nitric acid concentration column is 0.01 to 3.
- the number of theoretical plates of the NO recovery column is 5 to 30, the temperature at the top of the column is 30 to 120 ° C, the temperature of the column is 50 to 200 ° C, and the pressure at the top of the column is 1 to 10 MPa.
- the purge gas is fed from the 5th to 30th trays of the NO recovery tower; the concentrated nitric acid is fed from the 1st to 10th trays of the NO recovery tower; from the methanol separation tower The top recovered methanol is fed from the 1st to 10th trays.
- the molar ratio of NO in nitric acid, methanol, and purge gas is 1.1 ⁇ 10: 2 ⁇ 100: 1 ⁇ 5.
- the number of theoretical plates of the MN recovery column is 10 60
- the temperature at the top of the column is 0 to 50 ° C
- the temperature of the column is 0 to 80 ° C
- the reaction pressure is l 10 10 MPa.
- the number of theoretical plates of the DMO fine turret is 10 to 50, the temperature at the top of the column is 80 to 120 ° C, the temperature of the column is 120 to 200 ° C, and the operation is performed under normal pressure or reduced pressure.
- the DMO fine column has a light component reflux ratio of 0.1100.
- the composition of the purified gas recovered in the pressure swing adsorption tank is: N 2 is 60 to 80 v%, CO is 20 to 40 v%; and the separated C 2 2 gas accounts for 0.1 to 5 v% of the total amount of the intake air.
- the concentration of C0 2 is 99.8 to 99.9 v%; the separated CO 2 gas can be treated by an out-of-bounds device.
- the hydrogenation reactor is a plate reactor, a tubular reactor or a tubular-plate composite reactor.
- the hydrogenation plate reactor is a plate type fixed bed hydrogenation reactor.
- the center of the plate type fixed bed hydrogenation reactor is provided with a plate group fixing cavity, and the plate group fixed cavity is provided with a plate group; the plate group fixing cavity outer wall to the plate type fixed bed plus a catalyst bed is disposed between the inner walls of the hydrogen reactor; the catalyst bed is filled with a hydrogenation reaction catalyst; after the hydrogenation reaction raw material reaches the catalyst bed inlet temperature, from the top of the plate type fixed bed hydrogenation reactor The hydrogenation reaction takes place in the catalyst bed; the refrigerant introduced from the outside enters the plate group fixed cavity from the bottom of the plate-type fixed-bed hydrogenation reactor, and is taken out from the top of the plate-type fixed-bed hydrogenation reactor, and is subjected to a countercurrent process.
- the heat exchange takes away the heat of reaction of the hydrogenation reaction; the hydrogenation product from the bottom of the catalyst bed is withdrawn from the bottom of the plated fixed bed hydrogenation reactor.
- the plate type fixed bed hydrogenation reactor is connected with a steam drum II; the refrigerant introduced from the outside enters the steam drum II, and the refrigerant in the steam drum II enters the plate group fixed cavity of the plate type fixed bed hydrogenation reactor.
- the heat exchange with the catalyst bed removes the reaction heat; the heated refrigerant is a vapor-liquid mixture, enters the steam drum II for gas-liquid separation, and the generated low-pressure saturated steam enters the extra-low pressure steam recovery system for recycling.
- the refrigerant is water or a heat transfer oil, preferably water.
- the plate type fixed bed hydrogenation reactor is connected with a starting heater; at the initial stage of operation, the temperature does not reach the reaction requirement, and the hydrogenation reaction raw material enters the starting heater for preheating, and the preheating reaches the catalyst bed inlet temperature. Entering a catalyst bed for hydrogenation reaction; in the initial stage of operation, the starting heater provides a unique heat source for the hydrogenation reaction in the plate type fixed bed hydrogenation reactor; the heat source of the starting heater is a low pressure Steam.
- the hydrogenation reaction catalyst is selected from a commercially available catalyst of Shanghai Wuzheng Engineering Technology Co., Ltd., and the catalyst manufacturer brand name is MEG-801T.
- the number of theoretical plates of the methanol separation column is 10 to 40, the temperature at the top of the column is 40 to 70 ° C, the temperature of the column is 80 to 180 ° C, and the operation is performed under normal pressure or reduced pressure;
- the top light component reflux ratio is 0.1 ⁇ 3.
- the number of theoretical plates of the light component fine bismuth column is 10 to 60 pieces, the temperature of the top of the column is 58 to 90 ° C, the temperature of the column is 70 to 160 ° C, and the absolute pressure of the top of the column is 5 to 50 KPa.
- the light component reflux ratio of the light component fine column is from 1 to 50.
- the number of theoretical plates of the ethylene glycol product column is 30 to 100 pieces, the temperature of the top of the column is 100 to 150 ° C, the temperature of the column is 130 to 230 ° C, and the absolute pressure of the top of the column is 5 to 50 KPa;
- the reflux ratio of the light component of the top of the ethylene glycol product is 50-120 or full reflux.
- the membrane separator is composed of 1 to 100 hollow fiber membrane modules connected in parallel or in series.
- the membrane separator has a withstand pressure of 4.75 MPa, a maximum differential pressure of 1.5 MPa (raw gas to permeate), and a membrane separator operating temperature of up to 85 °C.
- the purified gas obtained by separation and purification by a membrane separator has a hydrogen concentration of 88 to 99.00 v% and a hydrogen recovery rate of 90 to 98.5%.
- the basic principle of the membrane separator is to use the partial pressure difference of the gas on both sides of the hollow fiber membrane as a driving force, and through the steps of the permeation-dissolution-diffusion-analysis, the hollow fiber membrane has different permeability to various gases. Thereby achieving the purpose of separation.
- the raw material gas moves away from the shell side of the hollow fiber membrane module, the permeate gas passes through the tube, and the exhaust gas enters the next hollow fiber membrane module.
- H 2 Since the permeation rate of H 2 on the surface of the membrane is several tens of times that of CH 4 , N 2 , Ar, etc., H 2 enters each hollow fiber tube and is collected from the lower portion of the membrane separator, and the non-permeate gas (exhaust gas) is removed from the hollow fiber membrane. The upper part of the assembly is discharged.
- the inside of the hollow fiber membrane module is a core member composed of 1000 to 100000 hollow fiber membranes, and the fiber tube is specially processed from a polymer material.
- the raw material gas enters from the side port of the separator. When the gas flowing downward along the outer side of the fiber bundle is in contact with the outer surface of the fiber membrane, the gas dissolves, penetrates and diffuses on the fiber wall, and utilizes various gases to dissolve and penetrate. Difference, separate different types of gases.
- the large-scale synthesis gas can be greatly reduced.
- the volumetric requirements of the alcohol process unit are conducive to the large-scale production of single-series units, which is conducive to safe production of equipment and reduced equipment investment.
- the nitric acid waste liquid recycling process and the purge gas recycling process are highly coupled, and the waste liquid generated in the device can be recycled as a raw material for recovering a large amount of nitrogen monoxide gas to generate a methyl nitrite required for the main reaction. .
- the technology of the process combination is scientific and reasonable, and the exhaust gas and waste liquid can be fully recycled through a reactor, which is economical and environmentally friendly.
- the methyl nitrite is a heat sensitive substance, especially after a certain temperature is higher, the temperature of the methyl nitrite is increased, and the reaction of CO carbonylation to dimethyl oxalate is strong.
- the thermal reaction using a suitable reactor to maintain a uniform temperature distribution of the bed and controlling the hot spot temperature is the key to preventing the decomposition of methyl nitrite and increasing the yield of the product.
- the carbonylation plate reactor of the present invention is a plate reactor.
- the reaction of CO carbonylation to dimethyl oxalate can fully utilize the characteristics of uniform temperature distribution of the reactor, and achieve the characteristics of increasing the space-time yield of dimethyl oxalate and recycling the heat of reaction.
- the recovery of the hydrogenation section of the process described in the process fully saves valuable hydrogen resources, thereby reducing the unit coal consumption, and is beneficial to reducing the overall energy consumption and pollution emissions of the device, which has practical significance.
- the process of the hydrogenation section of the process is recovered, and the membrane separation system used can reduce the pressure of the reaction system by about 1 MPa under the same load.
- the outlet pressure can be reduced, and a large amount of power consumption can be saved. .
- the membrane separation system is used, which is beneficial to increase the rate of hydrogenation reaction, and the daily output of ethylene glycol is increased by about 10%.
- the bottleneck of the large-scale device is effectively solved, the equipment investment is reduced, the heat recovery of the reaction heat is recovered, the effective heat recovery is performed, the energy consumption per unit of ethylene glycol production is reduced, steam is reduced, and cooling is performed.
- the invention realizes the full reuse of the exhaust gas and the waste liquid, the comprehensive energy utilization of the device reaction heat and the tower separation, improves the energy utilization efficiency, saves energy consumption, and has remarkable industrial application value.
- the invention provides a guarantee for the development of a more environmentally friendly, more efficient and more energy-saving technology for the synthesis gas glycol technology.
- the use of the invention is technically feasible and economically justifiable.
- the above process optimization design can significantly increase the yield, which has not been described in any literature.
- the process proposed by the invention is also particularly advantageous from the viewpoint of energy consumption, and has the characteristics of significant energy saving, and the combination should
- the use of a useful material recycling step, in particular, a nitric acid waste liquid recycling process and a high degree of coupling of the purge gas recycle process and its separation process and recycle of hydrogen in the reaction off-gas, the effect is very significant.
- Figure 1 An apparatus system for high-pressure carbonylation of industrial syngas to produce dimethyl oxalate and hydrogenated to ethylene glycol (part)
- Figure 2 Device system for high-pressure carbonylation of industrial syngas to produce dimethyl oxalate and hydrogenation to ethylene glycol (part)
- a system for the high-pressure carbonylation of industrial syngas to produce dimethyl oxalate and hydrogenate to ethylene glycol including a carbonylation reaction system, an esterification reaction system, and a gas-depleted waste acid coupling Recycling system to And a hydrogenation reaction system;
- the carbonylation reaction system comprises a carbonylation reactor 1, a first gas-liquid separator 4, a methanol scrubber 7, a methanol condensate column 5, and a DMO condensate column 6;
- the carbonylation reactor 1 is provided with a top feed port, a bottom discharge port, a bottom refrigerant inlet and a top refrigerant outlet;
- the first gas-liquid separator 4 is provided with a feed port, a gas outlet and a liquid outlet;
- the methanol scrubber 7 is provided
- the purge gas and waste acid coupling recovery system comprises a nitric acid concentration tower 12, a NO recovery tower 13, a MN recovery tower 15 and a pressure swing adsorption tank 16;
- the nitric acid concentration tower 12 is provided with a middle feed port, a top outlet and a bottom outlet;
- the NO recovery tower 13 is provided with a top feed port, a middle feed port, a bottom feed port, a top outlet, and a bottom outlet;
- the MN recovery column 15 is provided with an upper feed port, a lower feed port, a top outlet and a bottom outlet;
- the pressure swing adsorption tank 16 is provided with a feed port, a recovery gas outlet and an exhaust gas outlet;
- the hydrogenation reaction system comprises a hydrogenation cycle compressor 14, a hydrogenation reactor 17, and a second gas.
- the hydrogenation cycle compressor 14 includes an inlet and an outlet; and the hydrogenation plate reactor 17 a top feed port, a bottom discharge port, a bottom refrigerant inlet and a top refrigerant outlet; the second gas-liquid separator is provided with a feed port, a gas outlet and a liquid outlet; and the membrane separator 28 is provided with a feed Port, recovery gas outlet and vent gas outlet; the methanol
- the off-column 22 is provided with a middle feed port, a top non-condensable gas outlet, an upper liquid phase light component outlet and a bottom liquid phase heavy component outlet;
- the light component fine crucible tower 23 is provided with a lower feed port, a top outlet and a bottom outlet;
- the ethylene glycol product column 24 is provided with a lower feed port, a top outlet, an upper outlet and a bottom outlet; the top feed inlet of the carbonylation reactor
- the branch outlet A is connected to a lower feed port of the esterification reaction column 9 via a line, a branch outlet B and the NO recovery column 13 a bottom feed port is connected by a pipeline; a bottom outlet of the methanol scrubber 7 is connected to a lower feed port of the methanol condensate column 5; a top outlet of the methanol condensate column 5 and the esterification
- the upper feed port of the reaction column 9 is connected by a pipeline;
- the bottom outlet of the methanol condensate column 5 is connected to the lower feed port of the DMO fine sorghum column 6;
- the bottom outlet of the DMO fine boring tower 6 is
- the top feed port of the hydrogenation reactor 17 is connected by a pipeline, the top outlet of the DMO fine crucible tower 6 is a DMC product outlet; the other lower feed inlet of the esterification reaction tower 9 and the NO raw material pipeline and
- the raw material pipelines of the road 0 2 are respectively connected by pipelines; the top feed inlet of
- An inlet of the hydrogenation cycle compressor 14 is connected to an industrial hydrogen feedstock line via a line, and an outlet of the hydrogenation cycle compressor 14 is connected to a top feed port of the hydrogenation reactor 17 via a line;
- the bottom discharge port of the reactor 17 is connected to the feed port of the second gas-liquid separator via a pipeline;
- the gas outlet of the second gas-liquid separator is provided with a branch outlet G and a branch outlet H, and the branch outlet G and
- the inlet of the hydrogenation cycle compressor 14 is connected by a pipeline, and the branch outlet H is connected to the inlet of the membrane separator 28 via a pipeline;
- a liquid outlet of the second gas-liquid separator is connected to a lower feed port of the methanol separation column 22 via a line;
- a top non-condensing gas outlet of the methanol separation column 22 and a feed port of the membrane separator 28 Connected via a pipeline;
- the top liquid phase light component outlet of the methanol separation column 22 is provided with a
- the carbonylation reactor 1 is externally connected with a dehydration column 10; the dehydration column 10 is provided with a feed port and a dry gas outlet; a top outlet of the esterification reaction column 9 and the The recovery gas outlet of the pressure swing adsorption tank 16 is connected to the feed port of the dehydration column 10 via a line; the dry gas outlet of the dehydration column 10 is connected to the top feed port of the carbonation reactor 1 via a pipeline.
- the dehydration column is composed of two molecular sieve dryers A and molecular sieve dryers B which are alternately operated and regenerated; the molecular sieve dryer A and the molecular sieve dryer B are filled with an adsorbent.
- the bottom discharge port of the carbonylation reactor 1 is connected with an outlet heat exchanger I 3 ;
- the outlet heat exchanger I 3 is provided with a cold stream inlet, a cold stream outlet, and a hot material inlet.
- the CO feed line, the N 2 feed line, and the dry gas outlet of the dehydration column 10 are connected to the outlet of the outlet heat exchanger I 3 via a line;
- the cold stream of the outlet heat exchanger I 3 The outlet is connected to the top feed port of the carbonylation reactor 1 via a line;
- the bottom discharge port of the carbonylation reactor 1 is connected to the hot stream inlet of the outlet heat exchanger I 3 via a line;
- the hot stream outlet of the heat exchanger I 3 is connected to the feed port of the first gas-liquid separator 4 via a line.
- the carbonylation reactor 1 is externally connected with a steam drum I 2 ;
- the steam drum I 2 is provided with a refrigerant inlet, a refrigerant outlet, a vapor-liquid mixture inlet and a steam outlet;
- the refrigerant inlet of the refrigerant is connected to the refrigerant feed pipe via a pipeline;
- the refrigerant outlet of the steam drum I 2 is connected to the bottom refrigerant inlet of the carbonylation plate reactor 1;
- the top refrigerant outlet of the carbonylation reactor 1 is The steam drum 1 2
- the vapor-liquid mixture inlet is connected by a pipeline;
- the steam outlet of the steam drum 12 is connected to the outer steam recovery system via a pipeline.
- a carbonylation cycle compressor 8 is connected between the branch outlet A of the methanol scrubber 7 and the lower feed port of the esterification reaction column 9; the carbonylation cycle compressor 8 An inlet and an outlet are provided; the branch outlet A is connected to the inlet of the carbonylation cycle compressor 8 via a line; the outlet of the carbonylation cycle compressor 8 and the lower feed port of the esterification reaction column 9 are Pipeline connection.
- a top outlet of the NO recovery column 13 is connected to a bottom feed port of the MN recovery column 15 with a compressor 14; the compressor 14 is provided with an inlet and an outlet; The top outlet of the column 13 is connected to the inlet of the compressor 14 via a line; the outlet of the compressor is connected to the bottom feed port of the MN recovery column 15 via a line.
- the bottom discharge port of the hydrogenation reactor 17 is connected with an outlet heat exchanger ⁇ 20; the outlet heat exchanger II 20 is provided with a cold stream inlet, a cold stream outlet, and a hot material inlet. And a hot stream outlet; a bottom outlet of the DMO fine column 6, a recovery gas outlet of the membrane separator 28, and an outlet of the hydrogenation cycle compressor 25 and a cold stream inlet of the outlet heat exchanger Connected via a pipeline; a cold stream outlet of the outlet heat exchanger ⁇ 20 is connected to a top feed port of the hydrogenation reactor 17 via a line; a bottom discharge port of the hydrogenation reactor 17 is exchanged with the outlet
- the hot stream inlet of the heat exchanger ⁇ 20 is connected via a line; the hot stream outlet of the outlet heat exchanger ⁇ 20 is connected to the feed port of the second gas-liquid separator via a line.
- the top feed inlet of the hydrogenation reactor 17 is connected with a starter heater 19; the starter heater 19 is provided with a feed port and a discharge port; the outlet heat exchanger II
- the cold stream outlet of 20 is connected to the feed port of the starter heater 19 via a line; the discharge port of the starter heater is connected to the top feed port of the hydrogenation reactor 17 via a line.
- the hydrogenation reactor 17 is externally connected with a steam drum II 18; the steam drum II 18 is provided with a refrigerant inlet, a refrigerant outlet, a vapor-liquid mixture inlet and a steam outlet;
- the refrigerant inlet of 18 and the refrigerant feed pipe are connected by a pipeline;
- the refrigerant outlet of the steam drum II 18 is connected to the bottom refrigerant inlet of the hydrogenation reactor 17 via a pipeline;
- the top refrigerant outlet of the hydrogenation reactor 17 is The vapor-liquid mixture inlet of the steam drum 11 18 is connected by a line;
- the steam outlet of the steam drum II 18 is connected to the outer steam recovery system via a pipeline.
- the second gas-liquid separator comprises a high-pressure gas-liquid separator 21 and a low-pressure gas-liquid separator 26;
- the high-pressure gas-liquid separator 21 is provided with a feed port, a gas outlet and a liquid outlet
- the low-pressure gas-liquid separator 26 is provided with a feed port, a gas outlet and a liquid outlet;
- a bottom discharge port of the hydrogenation reactor 17 is connected to a feed port of the high-pressure gas-liquid separator 21 via a pipeline;
- the gas outlet of the high-pressure gas-liquid separator 21 is provided with a branch outlet K and a branch outlet L, and the branch outlet K is connected to the inlet of the hydrogenation cycle compressor 25 via a line, the branch outlet L and the low-pressure gas-liquid separator a feed port of 26 is connected by a line;
- a liquid outlet of the high-pressure gas-liquid separator 21 is connected to a middle feed port of the methanol separation column 22 via a line;
- the feed port of the membrane separator 28 is provided with a methanol absorption tank 27; the methanol absorption tank 27 is provided with a feed port and a purge gas outlet; and the low pressure gas-liquid separator 26 a gas outlet and a top non-condensable gas outlet of the methanol separation column 22 are connected to a feed port of the methanol absorption tank 27 via a line; a purge gas outlet of the methanol absorption tank 27 and the membrane separator 28
- the feed port is connected by a pipeline.
- the carbonylation reactor 1 may be a plate reactor, a tubular reactor or a tubular-plate composite reactor;
- the carbonylation reactor 1 is a plate type fixed bed carbonylation reactor; the center of the plate type fixed bed carbonylation reactor is provided with a plate group fixed cavity, and the plate group fixed cavity a plate group is disposed therein, the plate group fixing cavity is further provided with a bottom inlet and a top outlet; a catalyst bed layer is disposed between the outer wall of the plate group fixing cavity and the inner wall of the plate fixed bed carbonation reactor; The catalyst bed is filled with a carbonylation catalyst, and the catalyst bed is further provided with a top inlet and a bottom outlet; at the bottom of the plate fixed bed carbonylation reactor, the bottom refrigerant of the plate fixed bed carbonylation reactor The inlet is connected to the bottom inlet of the fixed portion of the plate group via a pipeline, and the bottom outlet of the catalyst bed is connected to the bottom discharge port of the plate fixed bed carbonylation reactor via a pipeline; At the top of the reactor, the top feed port of the plate fixed bed carbonylation reactor is connected to the top inlet of the catalyst
- the esterification reaction column 9 is a packed column; As a more preferred embodiment, the esterification reaction column 9 is a tray-filler mixing column having both a tray portion and a filler packed portion.
- the methanol scrubber 7, the methanol condensate column 5, the methanol recovery column 11, the NO recovery column 13, the MN recovery column 15, the DM0 fine column 6 and the nitric acid concentration column 12 are packed columns, Plate tower or bubble tower.
- the filler packed in the packed tower is a random packing or an efficient structured packing;
- the random packing is in the shape of a saddle shape, a Raschig ring, a Pall ring, a wheel shape, and a saddle. Ring, spherical or columnar;
- the high efficiency structured packing is corrugated packing, grid packing, pulse packing.
- the hydrogenation plate reactor 17 may be a plate reactor, a tubular reactor or a tubular-plate composite reactor;
- the hydrogenation reactor 17 is a plate type fixed bed hydrogenation reactor; the center of the plate type fixed bed hydrogenation reactor is provided with a plate group fixed cavity, and the plate group fixed cavity a plate group is disposed therein, the plate group fixing cavity is further provided with a bottom inlet and a top outlet; a catalyst bed layer is disposed between the outer wall of the plate group fixing cavity and the inner wall of the plate fixed bed hydrogenation reactor; The catalyst bed is filled with a hydrogenation reaction catalyst, and the catalyst bed is further provided with a top inlet and a bottom outlet; at the bottom of the plate fixed bed hydrogenation reactor, the plate type fixed bed hydrogenation reactor a bottom refrigerant inlet is connected to a bottom inlet of the plate group fixing chamber via a pipeline, and a bottom outlet of the catalyst bed is connected to a bottom discharge port of the plate type fixed bed hydrogenation reactor through a pipeline; At the top of the bed hydrogenation reactor, the top feed port of the plate fixed bed hydrogenation reactor is connected to the top inlet of the catalyst bed via
- the membrane separator 28 is composed of 1 to 100 hollow fiber membrane modules connected in parallel or in series.
- the NO from the line 18, the fresh methanol from the line 26, and the 0 2 of the 2 to 8 feeds are subjected to a gas-liquid countercurrent contact in the esterification reaction column 9 to effect an esterification reaction, and the MN mixture generated at the top of the column is passed through the line 23 It is combined with the recovered gas phase of the pressure swing adsorption tank from the pipeline 39, and then enters the dehydration tower 10 through the pipeline 24 for dehydration treatment, and the dehydrated dry gas is mixed with the CO from the pipeline 1 and the N 2 of the pipeline 2 through the pipeline 25 as The carbonation reaction feed gas enters the conduit 3.
- the column reactor in the esterification reaction column 9 is an acidic waste liquid containing a large amount of methanol, and is refluxed to the esterification reaction column 9 through a pipe 20 in a certain amount, and the remaining acid waste liquid passes through the pipe 21 and the methanol acid waste liquid from the pipe 33 at the same time.
- the methanol recovery tower 11 is introduced to carry out methanol recovery; the methanol light component generated at the top of the methanol recovery tower 11 is diverted through the pipeline 28, and part of it is passed through the pipeline 29 into the MN recovery tower 15 for washing liquid, and the other portions are merged from the pipeline 26
- the fresh methanol is passed through the line 22 as an alcohol source for the esterification reaction column 9; the acid-containing wastewater produced in the methanol recovery column 11 column is passed through a line 27 to the nitric acid concentration column 12 for nitric acid concentration.
- the carbonylation reaction starting material from the pipe 3 is exchanged with the carbonylation reaction product discharged from the bottom of the carbonylation reactor 1 through the outlet heat exchanger I 3 , and then enters the catalyst bed from the top of the carbonylation reactor 1 to carry out a carbonylation reaction.
- the purified water from outside the system enters the steam drum I 2 through the pipe 8, and the refrigerant in the steam drum I 2 passes through the pipe 9 from the bottom of the carbonation reactor 1 into the fixed space of the plate group to exchange heat with the catalyst bed, and is removed.
- the carbonation reaction product is subjected to heat exchange in the outlet heat exchanger I 3 and then enters the first gas-liquid separator 4 to be gas-liquid separated.
- the gas phase component containing most of the DMC (dimethyl carbonate) enters the methanol scrubber 7 through the pipe 11.
- the first gas-liquid separator 4 tower DMO heavy component via the pipeline 10 and the methanol scrubber 7 tower contains MN (methyl nitrite), DMC and DMO (dimethyl oxalate)
- MN methyl nitrite
- DMC dimethyl oxalate
- the methanol washing solution of the ester enters the methanol refining tower 5 through the pipe 12, and the two streams are countercurrently contacted for extraction separation; the gas phase light component of the top of the methanol scrubbing tower 7 is mostly passed through the carbonylation cycle compressor 8 through the pipeline 17
- the esterification reaction column 9 is recycled, and a small portion is taken as a purge gas through the pipeline 32 to the NO recovery tower 13 for recovery; the methanol and nitrite mixture recovered at the top of the methanol purification tower 5 is recycled to the esterification reaction through the pipeline 14.
- Tower 9 is reused, the heavy component of the tower is passed through the pipeline 13 into the DMO fine tower 6; the top of the DMO fine tower 6 is obtained from the DMC product, and the dimethyl oxalate component of the tower is introduced into the pipeline 15 as the original hydrogenation reaction. .
- the top of the nitric acid concentration tower 12 is mainly for the environmental treatment of the acid-containing wastewater discharged through the pipeline 30 to the boundary area, and the concentrated nitric acid concentrated at the bottom of the tower enters the NO recovery tower 13 through the pipeline 31 as an acid source and recovers methanol from the pipeline 57 and comes from
- the reversed-flow contact of the pipe 32 generates an esterification regeneration reaction to recover NO in the purge gas;
- the N 0 recovery tower 13 contains a methanol-containing nitric acid waste liquid which enters the methanol recovery tower 11 through the pipeline 33 for recycling.
- the resulting light component containing MN is pressurized by compressor 14 and passed to MN recovery column 15.
- the MN recovery column 15 is in countercurrent contact with the recovered methanol from the line 29, elutes the MN therein, and passes from the column tank through the line 36 to the esterification reaction column 9, and the overhead gas phase light component enters the pressure swing adsorption tank through the line 37. 16, after pressure swing adsorption, remove the CO-containing mixture after C0 2 through the pipeline
- the industrial hydrogen from the line 54 and the recycle gas from the line 53 are mixed, pressurized by the hydrocycling compressor 25, and then introduced into the line 55, and then mixed with the dimethyl oxalate component from the line 15 and the recovered hydrogen from the line 68 as Hydrogenation reaction feedstock, from line 40 to outlet heat exchanger 1120, and from the hydrogenation reactor
- the hydrogenation reaction product withdrawn at the bottom of 17 is subjected to heat exchange, and then enters the catalyst bed from the top of the hydrogenation reactor 17 to carry out catalytic hydrogenation reaction; at the same time, the purified water from outside the system enters the steam drum through the pipe 48.
- the refrigerant in the steam drum II 18 passes through the pipe 49 from the bottom of the hydrogenation reactor 17 into the fixed space of the plate group and exchanges heat with the catalyst bed, and the heat generated by the reaction is removed, and the heated refrigerant is a vapor-liquid mixture. After being taken out from the top of the hydrogenation reactor 17, it enters the steam drum ⁇ 18 for gas-liquid separation, and the generated low-pressure saturated steam enters the extra-low pressure steam recovery system through the pipeline 47 for recycling.
- the hydrogenation reaction product enters the high-pressure gas-liquid separator 21 from the pipeline 44 for gas-liquid separation, and the gas phase partially passes through the pipeline 51 and is mostly circulated as the recycle gas into the pipeline 53, and the remaining gas passes through the pipeline 52 to enter the low-pressure gas-liquid.
- the separator 26 performs gas-liquid separation; the liquid phase methanol in the low-pressure gas-liquid separator 26 flows out through the pipe 64, and the gas phase portion merges with the non-condensable gas from the pipe 58 through the pipe 65 and then enters the methanol absorption tank through the pipe 66.
- the liquid phase ethylene glycol crude product separated from the high pressure gas-liquid separator 21 flows out of the pipe 50, merges with the liquid phase methanol from the pipe 64, and enters the methanol separation column 22; the top of the methanol separation column 22 is suspended by the pipe 58.
- the amount of non-condensed steam is recovered, and the light component of the liquid phase in the top of the column enters the pipeline 57, and the liquid phase of the tower is passed through the pipeline.
- the polyol mixture is further purified through a conduit 59 into the ethylene glycol product column 24, wherein the mixed light components comprising 1,2-BDO and ethylene glycol are further recycled through line 63, and the lateral line of the tower body is produced.
- the ethylene glycol is produced as a product through line 62, which is treated as a mixture containing a small amount of ethylene glycol and ethylene glycol polycondensate to enter the boundary.
- the hydrogenation reaction raw material is heated by using the start-up heater 19, and the heat source is low-pressure steam.
- the hydrogenation feedstock from line 40 enters line 45 and is preheated to the bed inlet temperature by a starter heater 19 and then enters the catalyst bed from the top of hydrogenation reactor 17 via line 46 and line 42 for hydrogenation.
- the top light component from the methanol scrubber (composition: MN: 5.22 v%, CO: 22.12 v%, N 2: 58. 5 v%, NO: 11.14 v%, CO 2 : 0.63 v%, methanol 1.57 v% , Others: 0.82v%) and mixed with NO from the boundary to enter the esterification reaction tower 9 (inner diameter 50mm, height 2600mm, theoretical number of plates 25, tray structure is packed tower) from the 25th tray 0, 2 , 3 way from the 22nd, 23rd and 25th trays respectively into the esterification reaction tower 9, with fresh methanol fed from the first tray at the top of the tower and from the methanol recovery tower 11 Recovery of the methanol mixture, the fifth feed of the methanol and nitrite mixture recovered from the methanol refinery column 5, and the methyl nitrite-containing alcohol solution from the MN recovery column 15 column and feed from the 10th block
- the reflux of the column kettle is subjected to gas-liquid countercurrent contact in
- the temperature at the top of the esterification column 9 was 50 ° C, the temperature in the column was 93 ° C, the temperature in the reaction zone was 70 ⁇ 10 ° C, and the reaction pressure was 2 MPa.
- the esterification reaction column 9 was discharged from the column (composition: methanol: 71.8 wt%, MN: 8.0 wt%, and other heavy components such as acid and water formed by the reaction, 20.2 wt%), and after recovery, it was returned to the methanol recovery column 11 for recovery treatment.
- the gas phase component of the esterification reaction column 9 (composition: MN: 10.05 v%, CO: 26.42 v%, N 2 : 55.88 v%, NO: 5.2 v%, CO 2 : 0.60 v%, methanol 1.57 v%, Other: 0.28v %) then dehydrated into dehydration tower 10.
- adsorbent is 4A molecular sieve, operating temperature: 43 V: pressure: 1.9 MPa, alternating operation and regeneration of two molecular sieve dryers A and molecular sieve dryer B
- a dry gas having a water content of 60 ppm is obtained. .
- Esterification reaction tower 9 The acid-containing waste alcohol liquid in the column reactor enters the methanol recovery tower 11 (inner diameter 50mm, height 2100mm, theoretical plate number 20, built-in high-efficiency structured packing, tower top temperature 120 °C, bottom temperature 140 ° C, the pressure at the top of the column is 0.7 MPa, the reflux ratio of the light component at the top of the column is 1.2, and the top of the column is a light component containing methanol (component: methanol: 90 wt%, MN: 8 wt%, H 2 0: 2 wt %) a part (75% by weight) is combined with fresh methanol, enters the top of the esterification column 9, and remains as the washing liquid in the MN recovery column 15; the methanol recovery tower 11 contains the acid wastewater into the nitric acid concentration column 12 for nitric acid Concentrate.
- the methanol recovery tower 11 contains the acid wastewater into the nitric acid concentration column 12 for nitric acid Concentrate.
- the carbonylation reactor 1 (plate fixed bed reactor, inner diameter: 320 mm, height 2000 mm), the center is provided with a plate group fixed cavity, and the plate group fixed cavity is provided with 3 sets of plates, each set of 3 plates;
- a catalyst bed layer is disposed between the outer wall of the fixed cavity of the plate group and the inner wall of the carbonylation reactor 1, and the catalyst for carbonation high pressure reaction is loaded therein (commercially available catalyst of Shanghai Wuzheng Engineering Technology Co., Ltd., the catalyst brand name is DM0-0701T).
- the drying gas of the column 10 is mixed with the deuterated industrial grade CO (99 v%;) as a raw material for the carbonylation reaction and nitrogen as an inert gas source, and then exchanged with the carbonylation reaction product through the outlet heat exchanger 13 to preheat Heat to 95 °C, first enters from the top of the carbonylation reactor 1, and then enters the catalyst bed by radial flow to carry out carbonylation reaction (catalyst bed hot spot temperature 130 ° C, reaction pressure 1.8 MPa, gas hourly space velocity It is lOOOOh- 1 ); the carbonylation product then enters the outlet heat exchanger 3 for heat exchange and then enters the first gas-liquid separator 4 where it is subjected to gas-liquid separation.
- CO 99 v%
- the carbonylation reactor 1 is a fixed medium refrigerant medium.
- the purified water from the outside of the system enters the steam drum I 2 to be replenished into the water, and the water in the steam drum I enters the carbonization reactor 1 to exchange heat with the catalyst bed in the fixed cavity of the plate group, and removes the heat generated by the reaction, after heating
- the water is a vapor-liquid mixture, enters the steam drum for gas-liquid separation, and the generated low-pressure saturated steam is sent to the low-pressure steam pipe network outside the boundary area for recycling.
- the liquid phase (methanol: 1.16 wt%, DMC: 0.45 wt%, DMO: 97.6 wt%, other 0.79 wt%) drawn from the first gas-liquid separator 4 is used as an extractant to be separated into the methanol condensate column 5;
- the mixed gas phase component containing DMC enters the methanol scrubber 7 (internal diameter: 50mm, height is 3200mm, theoretical plate number is 30 pieces, and the high-efficiency structured packing is built in.
- the temperature at the top of the column is 28.1 °C, and the temperature of the column is 39.8 °C.
- the top pressure is 1.5 MPa.
- the DMC and DMO in the mixed gas are eluted, and most of the gas phase light components at the top of the methanol scrubber 7 pass through the carbonylation cycle.
- the compressor 8 enters the esterification reaction tower 9, and recycles the nitrogen oxides formed by the carbonylation reaction; a small portion of non-condensable gas (gas ratio: 0.5 v%) is taken as a purge gas into the NO recovery column 13 for recovery treatment; The liquid phase of the scrubber 7 column is passed into the methanol fine column 5 for separation.
- Methanol fine tower 5 (inner diameter: 50mm, height 2600mm, extraction precision tower, theoretical plate number is 25 pieces, with high-efficiency structured packing, tower top temperature is 73.12 °C, tower kettle temperature is 185.0 °C, tower top pressure
- the light component of the top of the O. lMPa) column (methanol: 88.2 wt%, MN: 11.8 wt%) enters the esterification reaction column 9 as one of the alcohol sources, and the heavy component of DMC and DMO enters the DMO fine Tower 6 is separated.
- DMO Fine Tower 6 (inner diameter: 50mm, height 3000mm, theoretical plate number 28, built-in high efficiency structured packing, tower top temperature 103 °C, column kettle temperature 180 ° C, atmospheric pressure operation, reflux ratio 50), tower
- the top DMC was collected as a product (DMC product purity was 99.41 wt%); the tower bottoms heavy component (DMO purity was 99.9 wt%) was used as the raw material for the hydrogenation section.
- the nitric acid concentration tower 12 (inner diameter 32mm, height 850mm, number of theoretical plates 8 pieces, high efficiency structured packing, peak temperature 64 ° C, column temperature 87 ° C, top pressure 0.15 MPa, reflux ratio 0.05) In the middle of the tower, the acid-containing wastewater is discharged to the outside of the boundary area for environmental protection treatment, and the concentration of the tower is concentrated to 68% by weight.
- the concentrated nitric acid serves as an acid source for the NO recovery column 13.
- NO recovery tower 13 (inner diameter: 32mm, height 2100mm, theoretical plate number 20, built-in high efficiency structured packing, tower top temperature 50 ° C, tower kettle temperature 100 ° C, tower top pressure 1.4 MPa)
- the purge gas from the methanol scrubber 7 is fed from the 20th tray, the recovered methanol (99.9 wt%) from the methanol separation column 22 fed from the first tray, and the 8th tower from the 8th column
- the esterification regeneration reaction occurs in countercurrent contact of concentrated nitric acid from the nitric acid concentration column 12 fed at the plate.
- the molar ratio of HN0 3 and methanol in the NO and concentrated nitric acid in the purge gas is 1:2.5:20.
- the top light component of the recovery column 13 (composition: CO: 21.1 v %, CO 2 : 0.6 v % , MN: 20.8v %, N 2 : 55.7 v %, methanol: 1.8 v %) Pressurized by compressor 14 into MN recovery tower 15; NO recovery tower 13 tower heavy component (composition: methanol 71.8wt%, reaction formation The other heavy components such as acid and water (28.2 wt%) were recovered into the third tray of the methanol recovery column 11.
- MN recovery tower 15 (inner diameter: 32mm, height 3200mm, theoretical plate number 30, built-in high efficiency structured packing, tower top temperature 30.8 ° C, tower kettle temperature 41.3 ° C, tower top pressure 2MPa)
- the material is countercurrently contacted with the recovered methanol from the methanol recovery column 11 fed from the first tray, and absorbs a large amount of paint in the intake air, and the remaining gas (composition: CO: 27.3v%, CO 2 : 0.8 v %, N 2: 71.9 v%,) from the top of the column into the pressure swing adsorption tank 16, the material in the column reactor (composition: methanol: 79.3 mol%, MN: 20.7mol %) of 5 proceeds esterification tray column 9 Recycling.
- the gas phase at the top of the MN recovery column 15 is pressure-adsorbed by the pressure swing adsorption tank 16, and the purified gas (N 2 : 72 v%, CO: 28 v%) is sent to the dehydration column 10 to be processed into the hydroformation reactor 1, and The 0.95 v% gas (composition: C0 2 is 99.8 v%) is discharged to the outside of the boundary for disposal.
- Hydrogenation reactor 17 (plate type fixed bed hydrogenation reactor, inner diameter: 325mm, height of 900mm), the center is provided with a plate group fixed cavity, and the plate group fixed cavity is provided with three sets of plates, each set of three plates
- the outer wall of the fixed cavity of the plate group is provided with a catalyst bed between the inner wall of the hydrogenation reactor, and the hydrogenation reaction catalyst is filled in: a commercially available catalyst of Shanghai Wuzheng Engineering Technology Co., Ltd., the catalyst brand name is MEG-801T).
- the material passing through the heat exchanger ⁇ 20 enters the starter heater 19 for preheating, and the preheated gas is used as the feed gas to reach the inlet temperature of the catalyst bed and then enters the catalyst bed for hydrogenation reaction.
- the cooling medium of the plate group is an aqueous medium.
- the refined water from the outside of the system enters the steam drum II 18 to be replenished into the water, and the water in the steam drum II 18 enters the hydrogenation reactor 17 to exchange heat with the catalyst bed in the fixed cavity of the plate group, and removes the heat generated by the reaction, after heating
- the water is a vapor-liquid mixture, and enters the steam drum II for gas-liquid separation.
- the generated low-pressure saturated steam is sent to the low-pressure steam pipe network outside the boundary area for recycling.
- the liquid phase separated by the low-pressure gas-liquid separator 26 enters the methanol separation column 22 for separation, and the gas phase is further removed by methanol through a methanol absorption tank 27 (inner diameter 160 mm, height 900 mm), wherein the gas phase (composition: hydrogen 97 v%, formazan) 0.15 v%, nitrogen 0.06 v%, carbon monoxide 0.27 v%, and other 2.52 v%) enter the membrane separator 28 for recycling.
- the hydrogen (purity of 99.9v%) separated by the membrane separator is preheated by the outlet heat exchanger and then enters the hydrogenation plate reactor 17, and only a small amount of non-condensable gas such as formazan is discharged as a purge gas. Recycling.
- Methanol separation tower 22 (inner diameter: 50mm, height 2600mm, theoretical plate number 25, built-in high efficiency structured packing, tower top temperature 50.82 ° C, tower kettle temperature 171 ° C, tower top absolute pressure 90 kPa) The material was fed at the 12th tray, and the top of the column was not condensed into the methanol absorption tank 27 and then passed to the membrane separator 28.
- the reflux ratio of the column was 1.6, and the top of the column was discharged (99.9 wt% methanol, 0.1 wt% other
- the low-boiling component is taken into the methanol scrubber 7 and the NO recovery column 13 respectively;
- the methanol separation column 22 is a heavy component of the column (composition: 96 wt% ethylene glycol, 0.12 wt% methyl glycolate, 2.68 wt% 1.2-BDO) , 0.8 wt% ethanol, 0.4 wt% other components) Enter the light component fine crucible tower 23.
- Light component fine crucible tower 23 (inner diameter: 50mm, height 4000mm, theoretical plate number 40, built-in high efficiency structured packing, tower top temperature 83.8 ° C, tower kettle temperature 146.9 ° C, tower top absolute pressure 16kPa, tower top With a reflux ratio of 50), the top of the column is taken out of the crude ethanol product (98 wt% ethanol, 2 wt% methyl glycolate) and sent to the outside of the boundary for collection and treatment; the heavy component of the column (97.9 wt% ethylene glycol, 2.1 wt% 1.2-BDO) ) Ethylene glycol product tower 24 in.
- Ethylene glycol product tower 24 (inner diameter 50mm, height 6500mm, tower theoretical plate number 60, built-in high efficiency structured packing, tower top temperature 130 ° C, tower kettle temperature 170.rC, tower top absolute pressure 5 kPa), tower The top reflux ratio is 98, and the top of the column is produced (component: 1, 2-BDO is 19.79 wt%; ethylene glycol is 80 wt%, other 0.21 wt%) is recovered as a by-product outside the boundary zone, and the column kettle contains a small amount of ethylene.
- the alcohol and ethylene glycol polycondensate were treated outside the boundary, and the final product ethylene glycol (content 99.99 wt%) was produced at the fifth tray of the side line of the ethylene glycol product tower.
Abstract
Description
Claims
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RU2016146715A RU2659069C1 (ru) | 2014-06-05 | 2014-07-23 | Способ и система устройств для получения диметилоксалата карбонилированием промышленного синтез-газа при средневысоком и высоком давлении и получения этиленгликоля гидрированием диметилоксалата |
CA2951165A CA2951165C (en) | 2014-06-05 | 2014-07-23 | Method and device system for producing dimethyl oxalate through medium and high-pressure carbonylation of industrial synthesis gas and producing ethylene glycol through dimethyl oxalate hydrogenation |
US15/316,178 US10017438B2 (en) | 2014-06-05 | 2014-07-23 | Method and device system for producing dimethyl oxalate through carbonylation of industrial synthesis gas and producing ethylene glycol through dimethyl oxalate hydrogenation |
SA516380431A SA516380431B1 (ar) | 2014-06-05 | 2016-12-05 | طريقة ونظام وسيلة لإنتاج أوكسالات داي ميثيل وإيثان-1، 2-ديول |
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AU2015203733B2 (en) * | 2014-07-03 | 2019-06-27 | China Petroleum & Chemical Corporation | Method for recycling methanol in the process of preparing dimethyl oxalate from synthesis gas |
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