176results about How to "Reduce the reflux ratio" patented technology

The invention provides an integrated internal circulation type denitrification and decarburization bio-membrane reactor and an operating method thereof. The main body of the reactor consists of an anoxic zone on the lower part, an aerobic zone on the upper part and a settling zone on the periphery of the aerobic zone; a composite filler is filled in the anoxic zone, and a water inlet pipe is communicated with the bottom of the anoxic zone; the aerobic zone is partitioned into a filler zone for adding a carrier on the upper part and a mud-water mixing zone on the lower part by adopting an orifice plate, the anoxic zone and the aerobic zone are partitioned through an impermeable partition plate, and a plurality of aeration pipes are arranged at the bottom of the aerobic zone and provided with air inlet pores; and the settling zone consists of three parts, namely a clean water zone, a contact settling zone and a sludge returning zone which are sequentially arranged from top to bottom, wherein the bottom of the sludge returning zone is provided with a sludge returning seam and communicated with the bottom of the aerobic zone. The reactor realizes zero power consumption in sludge returning, and is compact in structure; and a back flushing system is not required in the contact settling zone, and additional agents and carbon sources are not required, so that the reactor is low in running cost.

The invention discloses a technology for separating low carbon olefin gases, for solving the problems that hydrogen, methane, ethane and propane and other products with high purity can not be acquired and dimethyl ether and oxygen and carbon monoxide in impurities are not removed efficiently, etc. in the prior art. The technology is characterized in that a step of removing carbon monoxide and oxygen is added, methanol-to-olefin gas streams processed by removing carbon monoxide and oxygen enter into a deethanizing column, deethanizing column overhead streams successively pass through an ethene hydrogenation reactor, six separation pots, a low pressure demethanizing column and an ethene rectification column, etc. to separate to obtain ethene and ethane products, and deethanizing column bottom streams successively pass through a propyne hydrogenation reactor, a methane stripper and a propylene rectification column, etc. to separate to obtain propylene and propane products. According to the invention, polymer grade ethene and propylene products can be obtained, and hydrogen, methane, ethane and propane products, etc. with high purity can be obtained.

The invention belongs to a double-reflux denitrification membrane-bioreactor (MBR) process for treating dry acrylic fiber waste water, mainly aiming at treatment of high organic nitrogen with denitrification requirement and petrified dry acrylic fiber waste water which is difficult to degrade. The process comprises the following steps: feeding petrified dimethylformamide (DMF) dry acrylic fiber waste water into a front anoxic pool 2 from a water inlet 1, converting partial organic nitrogen into ammonia nitrogen under the anoxic condition, carrying out denitrification on a nitration liquid 10 refluxing to the front anoxic tank 2 by fully utilizing a waste water carbon source, and simultaneously compensating basicity 3 to the waste water; and then feeding entering the waste water into an aerobic pool 4, carrying out organism aerobic oxidation, organic nitrogen aerobic oxidation and ammonia nitrogen nitration under the abundant basicity, wherein the effluent contains a large amount of nitrates; refluxing the partial effluent to the front anoxic pool 2 for denitrification, and feeding the other effluent into a membrane separation pool 7; carrying out denitrification by utilizing an additionally arranged carbon source; and sucking with a micro-filter membrane assembly 8 so as to generate effluent 9, and refluxing a sludge concentrated liquid 11 to the front anoxic pool 2. The process is high in nitrogen removal efficiency.

The invention provides an AALOO multipoint water feeding synchronization denitrification and dephosphorization process. All pretreated wastewater Q1 enters an anaerobic tank, then flows through an anoxic tank, a low oxygen tank, a short-term aerobic tank and a precipitation tank sequentially, and then is discharged from the precipitation tank. Partial pretreated wastewater Q2 directly enters the low oxygen reaction tank, then flows through the short-term aerobic tank and the precipitation tank sequentially, and then is discharged from the precipitation tank. One part of precipitated sludge flows back to the anaerobic tank, and the other part of the precipitated sludge is discharged from the precipitation tank as excess sludge. Mixed liquid return channels are arranged between the low oxygen reaction tank and the anoxic tank, and the mixed liquid return channels are also arranged between the short-term aerobic tank and the low oxygen reaction tank. A returned sludge contact reaction region is arranged on the front end of the anaerobic tank, and water feeding points are arranged both on the front end region and the rear end region of the anaerobic tank. The method has a simple flow, and is adaptable to wastewater quality change, and is capable of removing nitrogen and phosphorus from wastewater with low carbon source and low oxygen consumption. The method is applicable to rebuilding or building of a municipal wastewater treatment plant which has nitrogen and phosphorus removing requirements.

The invention belongs to the field of chemical industry gas separation, and relates to a cracking gas separation method and a cracking gas separation apparatus. The method comprises: (1) pressurizingcracking gas; (2) cooling the compressed gas, and conveying to an absorption tower; (3) making the stream on the top of the absorption tower enter a re-absorption unit or be cooled, and conveying thestream on the tower kettle to a desorption tower; (4) obtaining C2 concentrated gas from the top of the desorption tower, obtaining a lean solvent from the tower kettle, and returning the lean solventto the top portion of the absorption tower; (5) making the C2 concentrated gas enter a purification unit, and purifying; (6) making the purified C2 concentrated gas enter a methane removing tower, and conveying the material from the kettle of the methane removing tower to an ethane removing tower; (7) obtaining crude ethylene gas from the top of the ethane removing tower, conveying the crude ethylene gas to an ethylene rectification tower, and extracting the material from the kettle of the ethane removing tower as a liquefied gas product or conveying to a propane removing tower; and (8) extracting a polymerization-grade ethylene product from the top/side line of the ethylene rectification tower, wherein the material from the tower kettle is an ethane-rich product. According to the presentinvention, the method and the apparatus have advantages of simple process, high recovery rate, low energy consumption and the like.

The invention relates to a process and a device for separating liquid-phase products of ethylene glycol from coal. The process includes respectively removing methanol and light components, then extracting ethylene glycol stream with heavy components by the aid of a reaction column of a propylene glycol and butylene glycol removal tower and acquiring ethylene glycol products by the aid of an ethylene glycol product tower; extracting ethylene glycol stream with propylene glycol and butylene glycol from a tower top of the propylene glycol and butylene glycol removal tower, carrying out acetal/ketal reactive distillation on the ethylene glycol stream with the propylene glycol and the butylene glycol, separating acetal/ketal products and then respectively carrying out hydrolysis and purification to obtain corresponding ethylene glycol, the corresponding propylene glycol and the corresponding butylene glycol. The process and the device have the advantages that the difficulty in removing propylene glycol and butylene glycol from ethylene glycol can be effectively lowered by means of applying acetal/ketal reaction, the reflux ratio and the total number of theoretical plates can be reduced, obvious energy conservation effects can be realized, and the quality of the thermal-sensitive ethylene glycol products can be guaranteed; the yield of the ethylene glycol products can be increased, and propylene glycol and butylene glycol products or butylene glycol acetal/ketal products further can be obtained by the aid of the method.

The invention relates to a method for separating glycol and 1,2-butanediol, which mainly solves the problems of high investment and energy consumption due to the fact that a very high reflux ratio and very high number of theoretical plates are required when a common rectification method is employed to separate and purify a material flow containing glycol and 1,2-butanediol, and severe separation conditions or a non-ideal separation effect when a common azeotropic rectification method is employed. The method better solves the problem by employing the technical scheme that the material flow containing glycol and 1,2-butanediol and a reactor enters from the upper part and the lower part of a reaction-azeotrope rectification tower respectively, a generated reaction product forms an azeotrope with glycol at the same time, a tower kettle obtains a material flow containing 1,2-butanediol, and after the azeotrope distilled from the tower top is subjected to condensation phase splitting, a glycol-rich phase at the lower layer is further refined to form a glycol product. The method can be used for industrial production of separating the material flow containing glycol and 1,2-butanediol.

The invention relates to a new energy-saving production process of ethyl acetate. The process comprises the sections of esterification, light removal, refining and recovery, and the membrane separation section is added between the esterification section and the light removal section. The organic phase at the esterification tower top is subject to membrane separation to desorb most moisture, and one part of the treated organic phase returns to an esterification tower to reflow and the other part is sent to a light removal tower to be refined. The membrane separation section comprises a vacuum cover (with a membrane module inside), a condenser, a penetrating fluid tank, a buffer tank and a vacuum pump. The method provided by the invention can greatly reduce water circulating in the esterification and light removal sections, save the heating steam in the esterification tower and the light removal tower, reduce the loads of the esterification tower and the light removal tower and further improve the production capability of the esterification tower and the light removal tower.

The invention relates to a separating method for ethylene-glycol and 1,2-butanediol and mainly solves the problems that when the ethylene-glycol and the 1,2-butanediol are separated and purified in the prior art, a common precise distillation method requires very high reflux ratio and theoretical plate number, resulting in large investment and high energy consumption; an azeotropic distillation method is harsh in separation condition and undesirable in separating effect. According to the method adopting the technical scheme that material flow containing the ethylene-glycol and the 1,2-butanediol enters into an azeotropic rectification column from the lower part and an azeotropic agent enters the azeotropic rectification column from the top to obtain an azeotrope of the ethylene-glycol and the azeotropic agent at the top, the material flow containing the 1,2-butanediol is obtained in a tower kettle; after the azeotrope is subjected to condensation and phase-splitting, the azeotropic agent-rich phase at the upper layer returns to the azeotropic rectification column and continues performing azeotropic reaction while an ethylene-glycol-rich phase at the lower layer is subjected to refining to obtain the ethylene-glycol product, and the problems are well solved. Therefore, the method can be used for industrial production for separating the ethylene-glycol and the 1,2-butanediol.

The invention discloses a method of separating catechol / hydroquinone in phenol hydroxylation reaction solution, which is characterized in that: phenol and hydrogen peroxide are reacted under catalyst action to produce reaction solution comprising water, phenol, catechol, hydroquinone and tar; vacuum rectification dehydration, de-phenol, catechol separating, hydroquinone separating and tar removing are made upon the reaction solution to prepare the catechol and the hydroquinone product; thermal medium oil independent circulation stepwise condensation / heat mode is adopted for the distillation system separating the catechol and the hydroquinone; vertical sieve plate is adopted for stripping section of the distillation tower; high-efficiency structured packing is adopted for the distillation section; embedded type structure in the tower is adopted for the condenser and the reboiler of the distillation tower. The method of separating catechol / hydroquinone in phenol hydroxylation reaction solution has the advantages of solving the problems of difficultly liquefying the catechol and the hydroquinone for the condenser at the top part of the distillation tower and easily causing material condensing or gasifying due to small difference value between the boiling point and the freezing point during vacuum rectifying for the catechol and the hydroquinone, prolonging production period, lowering unit consumption of product and reaching more than 99% for product purity of the catechol and the hydroquinone.

The invention discloses an epoxypropane refinement system which comprises an extraction tower, an extractant recovery tower and an epoxypropane rectification tower, wherein the middle part of the extraction tower is provided with an epoxypropane crude product inlet; the top of the extraction tower is provided with an extractant inlet; a tower bottom material outlet of the extraction tower communicates with a middle part material inlet of the extractant recovery tower; a tower top material outlet of the extractant recovery tower communicates with a middle part material inlet of the epoxypropane rectification tower; and the tower top of the epoxypropane rectification tower is provided with a high-purity epoxypropane material outlet. The system has the advantages of high product purity, low consumption, short process, less equipment and low investment.

The invention discloses a method for refining piperazine, which comprises the following steps of: adding piperazine reaction liquid in a tower of a rectifying column for heating separation; heating the reaction liquid in the tower to 130 DEG C-140 DEG C, controlling the reflux ratio to be 0.2-1:1, collecting 100 DEG C fractional water; continuing to heat to 140 DEG C -150 DEG C, controlling reflux ratio to be 2-5:1, collecting 119 DEG C fractional ethylene diamine; continuing to heat to 160 DEG C -170 DEG C, pumping an extraction agent into the rectifying column from an extraction agent inlet at the upper part of the rectifying column by using a microinfusion pump when the scale of a thermometer shows 140 DEG C, wherein the extraction agent is one of dihydric alcohol or triatomic alcohol of C2-C5; and controlling the reflux ratio to be 3-5:1, controlling the ratio of addition mass of the extraction agent per minute to extraction mass of piperazine per minute to be 0.05-0.2:1, and collecting 148 DEG C fractional piperazine which is pure piperazine. The method can improve the purity of the product and the separation efficiency and also can greatly reduce production cost since the extraction agent can be reused after being separated simply.

The invention belongs to the field of chemical engineering, and particularly discloses a method and a device for separating ethylene from refinery plant dry gas. The method comprises the steps of compression, purification, cooling, absorption, propane removal, methane removal, and ethylene refining. The method is based on a shallow cold oil absorption technology, directly produces a polymer-gradeethylene product from refinery plant dry gas on the premise that the refrigeration process is simplified, the cold consumption is reduced and the investment is saved, and has great industrial application prospects.

The invention provides an anaerobic-aerobic bio-filter coupled sewage processing device and a sewage processing method. The device comprises an anaerobic bio-filter, which is filled with an anaerobic filler layer that is covered by a bio-membrane containing anaerobic ammonia oxidation bacteria, anaerobic methanation bacteria, and denitrifying bacteria; an aerobic bio-filter, which is filled with an aerobic filler layer that is covered by a bio-membrane containing aerobic ammonia oxidation bacteria and nitrifying bacteria; an aeration device, which is arranged on the bottom of the aerobic bio-filter; a passive internal circulation device, which is arranged on the top of the aerobic bio-filter; and a backwater device, which comprises a backwater pipe and a backwater pump. The provided technical scheme couples the ammonia oxidization bacteria, methanation bacteria and denitrifying bacteria into a water treatment system, the methanation, ammonia oxidation, short-cut nitrification, and denitrification can be achieved synchronously, and thus the problems that in the biomembrane method, the contact efficiency between bacteria and sewage is low and the denitrification efficiency is low are solved effectively.

The invention provides an oxidation ditch membrane bioreactor, a wastewater treatment process and an application thereof. An oxidation ditch is arranged in the oxidation ditch membrane bioreactor; the oxidation ditch membrane bioreactor comprises an anoxic zone and an aerobic zone which are continuously arranged or an anaerobic zone, the anoxic zone and the aerobic zone which are continuously arranged; one or more membrane bio-reaction zones are arranged in the aerobic zone; a sewage inlet is arranged in the anoxic zone or the anaerobic zone; the membrane bioreactor is organically combined with the oxidation ditch; the advantages of S-MBR and R-MBR are fully utilized; sludge backflow is reduced or cancelled; the technical process and the power equipment are simplified; as S-MBR running, the oxidation ditch membrane bioreactor can realize in-situ online cleaning and soaking cleaning; as R-MBR running, the oxidation ditch membrane bioreactor can increase the land use rate and simplify operation and maintenance; an aerating system is optimized; the pulse aeration is combined for guaranteeing the valid oxygen demand in each zone, so that energy consumption waste is avoided. According to the invention, through the optimal combination of the reactor, the processing effect of nitrogen and phosphorus removal can be enhanced, the energy consumption can be saved and the land occupation can be saved.

The invention relates to a device and method for preparing high-purity nitrogen monoxide from adipic acid production tail gases. The device comprises a compressor, an absorption tower, an adsorption device, a low-temperature rectifying tower and a low-temperature refining tower which are connected in sequence, wherein the low-temperature rectifying tower is provided with an intercondenser; airflow discharged from the adsorption device enters the low-temperature rectifying tower after being cooled through a heat exchanger; purge gases located at the top of the tower and treated by the intercondenser is delivered to a tail gas treatment system after the cold energy is recovered; a liquid flow at the bottom of the tower enters the low-temperature refining tower; high-purity N2O is obtained from the top of the low-temperature refining tower and is filled after cold energy is recovered; a pressurized absorption, pressurized adsorption and low-temperature rectification coupling method is adopted; and the low-temperature rectifying tower is internally provided with an intercooler, so that the process energy consumption is greatly reduced on the premise that the high purity of the product is ensured.

The invention discloses a separation method of ethylene cracking gas through full temperature range-pressure swing adsorption and relates to the technical field of preparation of ethylene, propylene, hydrogen and the like and gas separation through pressure-swing adsorption. The separation method disclosed by the invention solves the problems existing in a sequential ethylene cracking gas separation (cryogenic distillation) method that the self energy of raw material gas cannot be fully utilized, the energy consumption in the separation process is higher, the product and recovery component purity or the yield are lower, and the like, and changes that a traditional pressure-swing adsorption method is only limited to the auxiliary effect of refined purification of ethylene tail gas and becomes basic separation unit operation as equally important as cryogenic distillation separation.

The invention relates to a method for separating 3, 4-dichloronitrobenzene from 2, 3-dichloronitrobenzene in 3, 4-dichloronitrobenzene crystallization mother liquor. Aiming at the characteristics of small isomer boiling point difference of the 3, 4-dichloronitrobenzene and the 2, 3-dichloronitrobenzene in low oil and difficulty in separation of the conventional method, alcohol, ketone, ester and aromatic hydrocarbon are used as an extraction agent to perform extractive distillation to obtain 3, 4-dichloronitrobenzene and 2, 3-dichloronitrobenzene distillates deviating from eutectic points, so that a foundation is laid for further purification.

The invention relates to a rectification-molecular sieve membrane coupling process and a rectification-molecular sieve membrane coupling device for separation of a ternary water-containing eutectic system, and discloses a novel separation device for direct coupling of a rectifying tower and a membrane component. The novel separation device comprises a tower internal component and a membrane permeation unit internal component contained in a conventional rectifying tower. For ternary water-containing system separation, a molecular sieve membrane steam permeation device and a rectifying tower areingeniously combined into a whole, separation of a ternary azeotropic system through a single rectifying tower of a simple structure is achieved, and the separation efficiency is obviously improved.