A production system for insoluble sulfur includes a polymeric kettle having a first discharge port and a quench tower (200) having a feed port. The first discharge port is in communication with the feed port. The quench tower has a cylindrical housing, a granulation device and a shear pump. A solvent inlet and a quenching agent inlet, which are respectively used for providing a solvent and a quenching agent, are arranged on the side wall of the housing. The sulfur production method includes raising the temperature of liquid sulfur under the protection of an initiator and nitrogen to perform polymerization reaction; introducing the polymerized material into the quenching tower and sequentially carrying out granulation and quenching treatment; carrying out solvent curing and extraction integrated treatment on the quenched product; and carrying out liquid phase circulating crushing and extraction integrated treatment on the cured and extracted product.

A gasification system according to an aspect includes a scrubber device to transfer contaminant contained in a flammable gas to cleaning water and discharge the cleaning water containing the contaminant as scrubber wastewater, a heat exchange device to heat the scrubber wastewater to vaporize the contaminant contained in the scrubber wastewater; and a combustion furnace to incinerate the vaporized contaminant, wherein the heat exchange device heats the scrubber wastewater by using heat generated by the combustion furnace.

A process for producing methane or methanol includes combining a hydrogenation catalyst, hydrogen, and CO.sub.2 with a condensed phase solution comprising an amine under conditions effective to form methane or methanol, and water. A process for coproduction of methanol and a glycol includes combining an epoxide, a hydrogenation catalyst, hydrogen, and CO.sub.2 with a condensed phase solution comprising an amine under conditions effective to form methanol and a glycol.

A method of continuously performing one or more heat-consuming processes, where at least one heat-consuming process is electrically heated. The maximum temperature in the reaction zone of the heat-consuming process is higher than 500° C., at least 70% of products of the heat-consuming process are continuously processed further downstream and/or fed to a local energy carrier network, and the electrical energy required for the heat-consuming process is drawn from an external power grid and from at least one local power source. The local power source is fed by at least one local energy carrier network and by products from the heat-consuming process. The local energy carrier network stores natural gas, naphtha, hydrogen, synthesis gas, and/or steam as energy carrier, and has a total capacity of at least 5 GWh. The local energy carrier network is fed with at least one further product and/or by-product from at least one further chemical process.

The polymerization process comprises polymerizing an olefin monomer and a comonomer in the presence of a polymerization catalyst in a polymerization step conducted in a polymerization reactor in a solvent to produce a solution comprising a polymer of the olefin monomer and the comonomer.

The polymerization process comprises withdrawing an exhaust stream of the solution from the polymerization reactor in a withdrawing step.

The polymerization process comprises separating the exhaust stream to a first primary stream and a primary concentrated solution stream in a first primary separation step, wherein the first primary stream comprises hydrocarbons and polymer.

The polymerization process comprises separating the first primary stream to a second primary stream and a third primary stream in a second primary separation step, wherein the second primary stream comprises dissolved polymer and the third primary stream comprises majority of the hydrocarbons.

The polymerization process comprises cooling the third primary stream to a temperature of −80 to 20° C. in a primary cooling step to obtain a cooled third primary stream.

The polymerization process comprises separating the cooled third primary stream to a fourth primary stream and a fifth primary stream in a third primary separation step, wherein the fourth primary stream comprises hydrocarbons in vapour phase and the fifth primary stream comprises liquid hydrocarbons.

The polymerization process comprises returning the fourth primary stream and the fifth primary stream independently in a primary returning step to a location upstream of the polymerization reactor.

Provided are integrated processes for she conversion of ethylene oxide to polypropiolactone. Systems for the production of polypropiolactone are also provided.

A device and a method for recovering by-product oxygen from water-electrolysis hydrogen production using a low-temperature method are provided, solving the waste problem of by-product oxygen in the green water-electrolysis hydrogen production system. The device according to the present disclosure comprises an oxygen clarifying system, a pressurizing and heat exchanging system, and a circulating gas compression and expansion refrigeration system. The recovering method according to the present disclosure comprises the following steps: first clarifying and purifying the by-product oxygen from water-electrolysis hydrogen production is to remove hydrogen, carbon monoxide, carbon dioxide, water and other impurities in the oxygen; and then, liquefying, pressurizing and heat exchanging the pure oxygen to obtain the product oxygen and liquid oxygen with required pressure. In the whole process, the cooling capacity is provided by the circulating gas expansion refrigeration system.

A composition contains an organopolysiloxane having the average chemical structure (I):

[R′R.sub.2SiO—(R.sub.2SiO).sub.m].sub.3—Si—[OSiR.sub.2].sub.n—Y—Si(OR).sub.3  (I)

where: R is independently in each occurrence selected from alkyl, aryl, substituted alkyl and substituted alkyl groups having from one to 8 carbon atoms; R′ is independently in each occurrence selected from R and terminally unsaturated alkylene groups having from 2 to 6 carbon atoms; Y is selected from a group consisting of: X, and X—(R.sub.2SiO).sub.pSiR.sub.2—X; where p has an average value in a range of one to 3; and X is independently in each occurrence selected from alkylene and substituted alkylene groups having from one to 6 carbon atoms; and the average values for subscripts m and n are each greater than zero and independently selected so that the average value for the sum of all of the average m values and the average n value is in a range of 30-200.

Wave-absorbing material powder of the present invention has oxidation resistance and salt fog resistance, which includes an iron-containing wave-absorbing material powder, and a metal oxide ceramic layer and a metal phosphate layer sequentially coated on an outside of the iron-containing wave-absorbing material powder from the inside to the outside. A method for preparing the wave-absorbing material powder includes using atomic layer deposition to coat the iron-containing wave absorbing material powder with a metal oxide ceramic coating, and then adopting the atomic layer deposition to coat the metal oxide ceramic coating with a metal phosphate layer; repeating the above steps to form an alternating nano-stack of the metal oxide ceramic coating and the metal phosphate layer outside the iron-containing absorbing material powder; and finally performing a high-temperature annealing treatment. The present invention improves temperature resistance, corrosion resistance and oxidation resistance of wave-absorbing materials.

A process produces sodium and/or potassium alkoxides in countercurrent by reactive rectification. Alcohol is reacted in countercurrent with the respective alkali metal hydroxide. The vapours containing alcohol and water are separated in at least two serially arranged rectification columns. The energy of the vapour obtained in the second rectification is utilized for operating the first rectification. This specific energy integration coupled with establishing a certain pressure difference in the two rectification stages makes it possible to cover a particularly large proportion of the energy required for the rectification through heating steam and minimizes the use of electricity.